CN108027199A - Method for producing liquefied natural gas - Google Patents

Method for producing liquefied natural gas Download PDF

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Publication number
CN108027199A
CN108027199A CN201680054318.5A CN201680054318A CN108027199A CN 108027199 A CN108027199 A CN 108027199A CN 201680054318 A CN201680054318 A CN 201680054318A CN 108027199 A CN108027199 A CN 108027199A
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CN
China
Prior art keywords
natural gas
nitrogen
gas flow
refrigeration cycle
flow
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN201680054318.5A
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Chinese (zh)
Inventor
迈克尔·A·特尼
欧里安·法尔吉斯
阿兰·吉亚尔
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority claimed from PCT/US2016/045811 external-priority patent/WO2017024235A1/en
Publication of CN108027199A publication Critical patent/CN108027199A/en
Pending legal-status Critical Current

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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
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—Nitrogen
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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"
    • F25J1/0035—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
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    • 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"
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    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
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    • F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
    • F25J1/008—Hydrocarbons
    • F25J1/0092—Mixtures of hydrocarbons comprising possibly also minor amounts of nitrogen
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    • F25J1/0208—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 a single-component refrigerant [SCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. with deep flash recycle loop
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    • 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
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    • 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
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    • F25J1/0238—Purification or treatment step is integrated within one refrigeration cycle only, i.e. the same or single refrigeration cycle provides feed gas cooling (if present) and overhead gas cooling
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Abstract

Provide a kind of method for producing liquefied natural gas.This method may include to provide high-pressure natural gas stream (2), the high-pressure natural gas stream is divided into Part I (102) and Part II (106), and the Part I of the high-pressure natural gas stream is liquefied to produce LNG stream (6).Refrigeration needed for cooling and liquefied natural gas by nitrogen kind of refrigeration cycle (6) and can depressurize the Part II of the high-pressure natural gas stream to provide.

Description

Method for producing liquefied natural gas
Related application
This application claims the U.S.Provisional Serial 62/201,947 submitted for 6th in August in 2015, in 2016 3 Month U.S. Provisional Patent Application No. 62/305,381 submitted for 8th and the U.S. Provisional Application sequence submitted for 4th in August in 2016 Numbers 62/370,953 priority, these provisional applications are all combined herein by quoting with its full text.
Technical field
Present invention relates in general to a kind of method for being used to effectively produce liquefied natural gas (LNG).
Background technology
Many places are using high pressure (transmission) network and lower pressure (distribution) network with natural through some areas supply Gas.Transmission network typically acts as the economically highway by natural gas long distance delivery to general area, and distributes network Serve as the highway of the personal user in natural gas transportation to some areas.The pressure of these networks changes because of place, but allusion quotation Offset is for transmitting between 30-80 absolute pressures and for distributing between 3-20 absolute pressures.Some applications are (for example, thermoelectricity joins Production, boiler etc.) there is the natural gas and other public utilities such as nitrogen of high flow capacity, it is depressurized with relative constant stream Consumer or secondary network are supplied under the conditions of amount, pressure and temperature.This pressure declines energy and is not often utilized.
Traditionally, natural gas is transported by compression and downwards along pipeline with by natural gas transportation to market under high pressure.Use High pressure to reduce the volume flow of natural gas, thus reduce pipe diameter (Capital expenditure) and/or with the relevant pressure of the pressure loss Contracting energy (operation expenditure).Pipeline operator also adapts to transient requirements by the use of high pressure as buffering.When natural gas has reached it During point of use, the pressure of natural gas is reduced to its final pressure for consumption in one or more control valves.From natural gas The utilisable energy that pressure reduces is wasted in control valve, any cooling as caused by natural gas flow by the flowing of these devices Effect (also referred to as Joule-Thomson effect) is same.Due to the relatively cool condition of gas downstream, such system is frequently necessary to heat Device and condensate system.
In the past, this wasted energy is utilized by using the energy of natural gas expansion and the facility of refrigeration effect is made.One kind is so Facility be Cryo Equipment department (Airco Industrial Gases ' Cryoplants by Airco industrial gases companies Division) design and build for UGI companies in Lei Ding cities of Pennsylvania in earlier 1970s.It is used Natural gas letdown station (" pressure-reducing station ") manufactures liquefied natural gas (" LNG ") or liquid nitrogen (" LIN ").Under high pressure from transport pipeline Most of natural gas into factory is cooled and is sent to expansion turbine, and energy and refrigeration are produced in the expansion turbine.Then Remaining stream is cooled down with refrigeration, and a part is liquefied.Then using the liquefied storage tank that is partially transferred to as LNG product.Will Not liquefied heated by natural gas, the low-pressure manifold collected and be sent under the pressure lower than high-pressure main.
U.S. Patent number 6,196,021 describe it is a kind of using natural gas expansion come provide refrigeration with liquefied natural gas stream Then system, the natural gas flow are vaporized to cool down nitrogen stream by carrying out heat exchange with nitrogen stream.This refrigeration supplements The refrigeration provided with nitrogen circulation is declined by nitrogen pressure to provide liquid nitrogen.Similarly, U.S. Patent number 6,131,407 describe A kind of system, which, which produces, needs the LIN for being directly sent to air gas separation unit (" ASU ") to aid in the refrigeration of ASU.The U.S. is special Sharp application publication number 2014/0352353 describes the similar system of the system disclosed with U.S. Patent number 6,131,407, still Add, caused LIN can be sent to tank without being used to liquid auxiliary ASU.In each of these systems, LNG is re-vaporized to provide nitrogen cooling.It is not intended, however, that be to liquefy and then re-vaporize natural gas because this is heat Efficiency is low.U.S. Patent number 6,694,774 describes a kind of system, which is freezed to produce using natural gas depressurization to provide Raw liquefied natural gas stream, wherein freezing by closed loop mixed-refrigerant cycle to supplement.
Fig. 1 provides the process flow chart of typical small-sized LNG schemes, and the program is using in the closed including nitrogen compression The nitrogen circulation 50 of machine 10, cooler 11,21,26 and the first and second turbocharger 20,25.For mesh discussed herein , turbocharger is the combination of turbine and booster, and wherein booster provides power by turbine at least in part, the turbine allusion quotation Realized via common axis type.Natural gas 2 is purified first in purification unit 30 equipment is damaged during liquefaction or is freezed Component.Then the natural gas 4 of purifying is cooled down in heat exchanger 40, use is by nitrogen kind of refrigeration cycle 50 in the heat exchanger The refrigeration of offer condenses the steam into LNG 6.Typically, by adsorb, distill or gas-liquid separator exchanger 40 interposition Heavy hydrocarbon (pentane and more heavy hydrocarbon) is removed before putting or since the centre position from natural gas, to prevent these components from exchanging Freeze in device 40.In the example of fig. 1, the centre portion of natural gas 4 from heat exchanger 40 is extracted, to use gas-liquid point Heavy hydrocarbon 8 is removed from device 5.In the exemplary device shown in Fig. 1, it is about 7155kW to produce the power needed for the LNG of 342mtd, this meaning The specific power that taste this device is about 502kWh/mt.
Thus, it would be advantageous to provide operation is so as to produce the method for the LNG of lower cost and set in a more effective manner It is standby.
The content of the invention
The present invention is at least one method and apparatus met in these demands.In certain embodiments, it is of the invention It can provide a kind of for producing the lower cost of LNG, more effective and more flexible method.For example, in certain embodiments, this Invention can also include the co-production of liquid nitrogen (" LIN ").In the additional examples, the present invention can include based on power into This, product requirements and/or level of supply change the productivity of any one of LIN and LNG or both.
Because the relatively low cost of transportation with the volume flow of the relevant reduction of gases at high pressure, nitrogen are defeated by pressure piping Send.Typically, such pipeline is run in the range of 30 to 50 absolute pressures.Usually it is not required to using the user of the nitrogen from pipeline Nitrogen that will be at these pressures.For example, nitrogen is used as inertia effectiveness stream typically under the pressure in the range of 3 to 8 absolute pressures Body.Therefore, it is wasted in these places, potential refrigerating capacity.In addition, there are still the following situations, wherein to pipe feed The production device of nitrogen cannot be run with 100% equipment design capacity, and therefore, or large-scale nitrogen compressor is not run, Do not run under optimum capacity.If, can this thing happens for example, be less than initial expection to the demand of nitrogen. It is because nitrogen produces equipment and is sized to meet in peak value operating condition, environment bar another reason for such case occur Peak user demand under part, catalyst life etc..Therefore, when other systems do not adapt to increased load, nitrogen produces Equipment is designed to underuse during many operating conditions.
In certain embodiments of the present invention, gas decompression by using natural gas depressurization and nitrogen or rich in nitrogen Refrigerating capacity, a kind of method can provide LNG and/or LIN with the energy input of at least reduction and produce.Example rich in nitrogen is Having less than 12%O2The poor synthesis of air stream of (for example, combustion limits due to the mixture with methane).In embodiment, Decompression process occurs in the decompression close to both the place of existing utility or generation natural gas and nitrogen to meet facility demand Place so that with not utilizing air-flow (for example, nitrogen stream, the gas stream rich in nitrogen or natural gas or its in production site His high pressure draught) the situation of decompression compare, LNG and/or LIN can be produced with the operating cost of reduction and/or capital cost.
In one embodiment, the present invention can include a kind of method for being used to produce liquefied natural gas (" LNG ").One In a embodiment, this method may comprise steps of：A) nitrogen kind of refrigeration cycle is provided, the wherein nitrogen kind of refrigeration cycle is configured as Refrigeration is provided in heat exchanger；B) the first natural gas flow is purified in the first purification unit to remove first group of impurity, so as to produce First natural gas flow of raw purifying；C) cool down using the refrigeration from the nitrogen kind of refrigeration cycle in the heat exchanger and liquefy this First natural gas flow is to produce LNG stream, and wherein first natural gas flow has LNG refrigeration demands, and wherein the LNG stream is in the first pressure Power PHLower liquefaction；D) the second natural gas flow is purified in the second purification unit to remove second group of impurity, so as to produce purifying Second natural gas flow；E) second natural gas flow is partly cooled down in the heat exchanger；F) from the middle area of the heat exchanger Section extracts the second natural gas flow of part cooling；G) the second natural gas for cooling down in natural gas expansion turbine the part Stream is expanded into middle pressure PMTo form cold natural gas flow, wherein P is pressed in thisMIn less than first pressure PHPressure；And h) exist The cold natural gas flow is heated with the heat of the heat exchanger by carrying out heat exchange with first natural gas flow in the heat exchanger End produces the natural gas flow of heating, and the wherein natural gas expansion turbine drives the first booster, wherein the LNG refrigeration demand origin There is provided from the combination of the nitrogen kind of refrigeration cycle and the refrigeration of step h).
In the optional embodiment of the method for producing LNG：
● first booster is configured to compress second natural gas flow or the stream from second natural gas flow.
● first booster is configured to compress stream selected from the group below, which is made of the following：First natural gas flow, Natural gas flow, second natural gas flow, the second natural gas flow of the purifying, the natural gas of part cooling of first purifying Flow, the nitrogen fluid in the natural gas flow and the nitrogen kind of refrigeration cycle of the heating；
● first group of impurity is in first pressure PHThe solidification point of the lower condensing temperature with or greater than methane；
● second group of impurity includes water；
● the nitrogen kind of refrigeration cycle includes recycle compressor, turbine, booster and multiple coolers, the wherein turbine and booster It is configured so that the turbine is configured to the booster and provides power；
● first natural gas flow and second natural gas flow come from same gas source；
● the gas source is the natural gas line with the pressure between 15 and 100 absolute pressures；
● first natural gas flow comes from the first gas source, and second natural gas flow comes from the second gas source, wherein First gas source and second gas source are different sources；
● first gas source includes natural gas line；
● the natural gas line has the pressure between 15 and 100 absolute pressures；
● first purification unit and second purification unit are same units；And/or
● first purification unit and second purification unit are separated units, wherein first purification unit be configured to Water and carbon dioxide are removed less, and wherein second purification unit is configured at least remove water.
In another aspect of the invention, there is provided one kind is used for the method for producing liquefied natural gas (" LNG ").At this In embodiment, this method comprises the following steps：A) nitrogen kind of refrigeration cycle is provided；B) in a heat exchanger by with freezing from the nitrogen The nitrogen of circulation carries out heat exchange come first natural gas flow that cools down and liquefy to produce LNG stream, and wherein the LNG stream is in first pressure Lower liquefaction；C) the second natural gas flow is made to be expanded into second pressure to produce the natural gas flow of expansion；And d) in the heat exchanger The middle natural gas flow for heating the expansion to produce the natural gas flow of heating, wherein step d) provide be used to cooling down and liquefy this first A part for the refrigeration of natural gas flow.
In the optional embodiment of the method for producing LNG：
● first natural gas flow comes from the first gas source, and second natural gas flow comes from the second gas source, wherein First gas source and second gas source are different sources；And/or
● in step b) liquefied first gas source in the natural gas flow of the expansion, wherein the first pressure and this Two pressure are roughly the same.
In another aspect of the invention, there is provided one kind is used for the method for producing liquefied natural gas (" LNG ").At this In embodiment, this method comprises the following steps：A) high-pressure natural gas stream is provided；B) the high-pressure natural gas stream is divided into Part I And Part II；C) Part I of cooling and the high-pressure natural gas stream that liquefies is to produce LNG stream；D) via nitrogen kind of refrigeration cycle First refrigerating part is provided, wherein the nitrogen kind of refrigeration cycle includes recycle compressor, turbine, booster and multiple coolers, wherein The turbine and booster are configured so that the turbine is configured to the booster and provides power；E) by making the high pressure day The Part II of right gas is expanded to provide the second refrigerating part；And f) using first refrigerating part and second refrigeration section Divide the cooling and liquefaction of the Part I to realize the high-pressure natural gas stream in step c).
In another aspect of the invention, there is provided one kind is used to produce liquefied natural gas (" LNG ") and liquid nitrogen (" LIN ") Method.In this embodiment, this method may comprise steps of：A) nitrogen kind of refrigeration cycle is provided, wherein nitrogen refrigeration is followed Ring is configured to provide refrigeration in heat exchanger, and a part for the wherein nitrogen in the nitrogen kind of refrigeration cycle is extracted and liquefies Liquid nitrogen product is produced, wherein the gaseous nitrogen of at least moiety is incorporated into the nitrogen kind of refrigeration cycle according to former state is extracted；B) exist The first natural gas flow is purified in first purification unit to remove first group of impurity, so as to produce the first natural gas flow of purifying；c) In the heat exchanger first natural gas flow is cooled down and liquefied to produce LNG using the refrigeration from the nitrogen kind of refrigeration cycle Stream, wherein first natural gas flow has LNG refrigeration demands, and wherein the LNG stream is in first pressure PHLower liquefaction；D) it is pure second Change in unit and purify the second natural gas flow to remove second group of impurity, so as to produce the second natural gas flow of purifying；E) in the heat Second natural gas flow is partly cooled down in exchanger；F) the of part cooling is extracted from the centre portion of the heat exchanger Two natural gas flows；G) the second natural gas flow that the part cools down is made to press P in being expanded into natural gas expansion turbineMIt is cold to be formed Natural gas flow, wherein presses P in thisMIn less than first pressure PHPressure；And h) in the heat exchanger by with this One natural gas flow carries out heat exchange and heats the cold natural gas flow to produce the natural gas flow of heating in the hot junction of the heat exchanger, its In the natural gas expansion turbine drive the first booster, wherein the LNG refrigeration demands are by from the nitrogen kind of refrigeration cycle and step h) Refrigeration combination provide.
In the optional embodiment of the method for producing LNG and LIN：
● first booster is configured to compress second natural gas flow or the stream from second natural gas flow.
● first booster is configured to compress stream selected from the group below, which is made of the following：First natural gas flow, First natural gas flow of the purifying, second natural gas flow, the second natural gas flow of the purifying, the natural gas of part cooling Flow, the nitrogen fluid in the natural gas flow and the nitrogen kind of refrigeration cycle of the heating；
● the liquid nitrogen product has a LIN refrigeration demands, and wherein the LIN refrigeration demands are by from the nitrogen kind of refrigeration cycle and step h) The combination of refrigeration provides；
● first group of impurity is in first pressure PHThe solidification point of the lower condensing temperature with or greater than methane；
● second group of impurity includes water；
● the nitrogen kind of refrigeration cycle includes recycle compressor, turbine, booster and multiple coolers, the wherein turbine and booster It is configured so that the turbine is configured to the booster and provides power；
● the nitrogen kind of refrigeration cycle further includes nitrogen feed compressor；
● first natural gas flow and second natural gas flow come from same gas source；
● the gas source is the natural gas line with the pressure between 15 and 100 absolute pressures；
● first natural gas flow comes from the first gas source, and second natural gas flow comes from the second gas source, wherein First gas source and second gas source are different sources；
● first gas source includes natural gas line；
● the natural gas line has the pressure between 15 and 100 absolute pressures；
● first purification unit and second purification unit are same units；
● first purification unit and second purification unit are separated units, wherein first purification unit be configured to Water and carbon dioxide are removed less, and wherein second purification unit is configured at least remove water；And/or
● the liquefaction of nitrogen device further includes subcooler.
In another aspect of the invention, there is provided one kind is used to produce liquefied natural gas (" LNG ") and liquid nitrogen (" LIN ") Method.In this embodiment, this method may comprise steps of：A) nitrogen kind of refrigeration cycle is provided, wherein nitrogen refrigeration is followed Ring is configured to provide refrigeration in heat exchanger, and a part for the wherein nitrogen in the nitrogen kind of refrigeration cycle is extracted and liquefies Liquid nitrogen product is produced, wherein the gaseous nitrogen of at least moiety is incorporated into the nitrogen kind of refrigeration cycle according to former state is extracted；B) exist In heat exchanger the first natural gas flow is cooled down and liquefied to produce by carrying out heat exchange with the nitrogen from the nitrogen kind of refrigeration cycle Raw LNG stream, the wherein LNG stream liquefy at the first pressure；C) the second natural gas flow is made to be expanded into second pressure to produce expansion Natural gas flow；And the natural gas flow of the expansion d) is heated in the heat exchanger to produce the natural gas flow of heating, wherein Step d) provides a part for the refrigeration for first natural gas flow that cools down and liquefy.
In the optional embodiment of the method for producing LNG and LIN：
● first natural gas flow comes from the first gas source, and second natural gas flow comes from the second gas source, wherein First gas source and second gas source are different sources；
● the liquid nitrogen product has a LIN refrigeration demands, and wherein the LIN refrigeration demands are by from the nitrogen kind of refrigeration cycle and step d) The combination of refrigeration provides；And/or
● in step b) liquefied first gas source in the natural gas flow of the expansion, wherein the first pressure and this Two pressure are roughly the same.
In another aspect of the invention, there is provided one kind is used to produce liquefied natural gas (" LNG ") and liquid nitrogen (" LIN ") Method.In this embodiment, this method may comprise steps of：A) nitrogen kind of refrigeration cycle is provided, wherein nitrogen refrigeration is followed Ring includes recycle compressor, turbine, booster and multiple coolers, and the wherein turbine and booster is configured so that the whirlpool Wheel is configured to the booster and provides power, and a part for the wherein nitrogen in the nitrogen kind of refrigeration cycle is extracted and production of liquefying Raw liquid nitrogen product, wherein the gaseous nitrogen of at least moiety is incorporated into the nitrogen kind of refrigeration cycle according to former state is extracted；B) provide High-pressure natural gas stream；C) the high-pressure natural gas stream is divided into Part I and Part II；D) cooling and the high pressure that liquefies are natural The Part I of air-flow is to produce LNG stream；E) the first refrigerating part is provided via the nitrogen kind of refrigeration cycle；F) by making the high pressure The Part II of natural gas is expanded to provide the second refrigerating part；And g) using first refrigerating part and second refrigeration Realize the cooling and liquefaction of the Part I of the high-pressure natural gas stream in step d) in part.
In another aspect of the invention, there is provided one kind is used for liquefaction of nitrogen device and natural gas liquefaction device integration with life The method for producing liquefied natural gas (" LNG ") and liquid nitrogen (" LIN ").In this embodiment, this method may comprise steps of： A) the liquefaction of nitrogen device with the first nitrogen kind of refrigeration cycle is provided, the wherein liquefaction of nitrogen device includes turbine, booster and multiple cold But device, wherein the first nitrogen kind of refrigeration cycle are configured to provide refrigeration in first heat exchanger；B) the second nitrogen refrigeration is provided to follow Ring, wherein the second nitrogen kind of refrigeration cycle include the second turbine, the second booster and multiple second coolers, the wherein second nitrogen system SAPMAC method is configured to provide refrigeration in second heat exchanger；C) purified in the first purification unit the first natural gas flow with except First group of impurity is removed, so as to produce the first natural gas flow of purifying；D) use in the second heat exchanger and freeze from the nitrogen The refrigeration of circulation is come first natural gas flow that cools down and liquefy to produce LNG stream, and wherein first natural gas flow freezes with LNG Demand, wherein the LNG stream is in first pressure PHLower liquefaction；E) the second natural gas flow is purified in the second purification unit to remove Two groups of impurity, so as to produce the second natural gas flow of purifying；F) it is second natural that this is partly cooled down in the second heat exchanger Air-flow；G) natural gas flow of part cooling is extracted from the centre portion of the second heat exchanger；H) whirlpool is expanded in natural gas The natural gas flow that the part cools down is set to be expanded into middle pressure P in wheelMTo form cold natural gas flow, wherein P is pressed in thisMIn less than this First pressure PHPressure；And i) should by carrying out heat exchange heating with first natural gas flow in the second heat exchanger To produce the natural gas flow of heating in the hot junction of the second heat exchanger, the wherein natural gas expansion turbine drives cold natural gas flow First booster, wherein the LNG refrigeration demands are provided by the combination from the second nitrogen kind of refrigeration cycle and the refrigeration of step i), its In extract the part of liquid nitrogen in the first nitrogen kind of refrigeration cycle as product liquid nitrogen, wherein the gas by least moiety State nitrogen shines to extract as product liquid nitrogen to be incorporated into the first nitrogen kind of refrigeration cycle as former state, and wherein the first nitrogen kind of refrigeration cycle A common nitrogen recycle compressor is shared with the second nitrogen kind of refrigeration cycle.
In for the optional embodiment of liquefaction of nitrogen device and the integrated method of natural gas liquefaction device：
● first booster is configured to compress second natural gas flow or the stream from second natural gas flow.
● first booster is configured to compress stream selected from the group below, which is made of the following：First natural gas flow, First natural gas flow of the purifying, second natural gas flow, the second natural gas flow of the purifying, the natural gas of part cooling Flow, the nitrogen fluid in the natural gas flow and the nitrogen kind of refrigeration cycle of the heating；First group of impurity is in first pressure PHLower tool There is the solidification point of the condensing temperature at or greater than methane；
● second group of impurity includes water；
● the first nitrogen kind of refrigeration cycle further includes nitrogen feed compressor；
● the first nitrogen kind of refrigeration cycle is the kind of refrigeration cycle of closing；
● first natural gas flow and second natural gas flow come from same gas source；
● the gas source is the natural gas line with the pressure between 15 and 100 absolute pressures；
● first natural gas flow comes from the first gas source, and second natural gas flow comes from the second gas source, wherein First gas source and second gas source are different sources；
● first gas source includes natural gas line；
● the natural gas line has the pressure between 15 and 100 absolute pressures；
● first purification unit and second purification unit are same units；
● first purification unit and second purification unit are separated units, wherein first purification unit be configured to Water and carbon dioxide are removed less, and wherein second purification unit is configured at least remove water；And/or
● the liquefaction of nitrogen device further includes subcooler.
In another aspect of the invention, there is provided one kind is used for the first liquefier and the second liquefier integration to produce The method of first liquefied gas and the second liquefied gas.In this embodiment, this method may comprise steps of：A) providing has First liquefier of the first kind of refrigeration cycle, wherein first liquefier include recycle compressor, first heat exchanger and turbine Booster；B) second kind of refrigeration cycle is provided, wherein second kind of refrigeration cycle is configured to provide refrigeration in second heat exchanger, C) in the second heat exchanger by carrying out heat exchange with second kind of refrigeration cycle the first air-flow is cooled down and liquefied to produce Liquefied first air-flow, wherein liquefied first air-flow are in first pressure；D) make the second flow expansion to second pressure with Produce the second air-flow of expansion；And the second air-flow of the expansion e) is heated in the second heat exchanger to produce the gas of heating Stream, the first refrigerant gas is produced wherein extracting and liquefying a part for the first refrigerant gas in first kind of refrigeration cycle Product liquid, wherein using the first refrigerant gas of gaseous state of at least moiety according to the product liquid extraction as the first refrigerant gas Go out and be incorporated into as former state in first kind of refrigeration cycle, wherein in addition to the refrigeration provided by second kind of refrigeration cycle, step e) is carried The refrigeration for first air-flow that cools down and liquefy is supplied, and wherein first kind of refrigeration cycle and second kind of refrigeration cycle shares One common recycle compressor.
In for the optional embodiment of the first liquefier and the integrated method of the second liquefier：
● first kind of refrigeration cycle is selected from the group being made of nitrogen kind of refrigeration cycle and hydrogen kind of refrigeration cycle；
● in step c) liquefied first air-flow derive from the expansion the second air-flow, wherein the first pressure and this second Pressure is roughly the same；
● second kind of refrigeration cycle is selected from the group being made of nitrogen kind of refrigeration cycle and hydrogen kind of refrigeration cycle；
● cooling and liquefied first air-flow include natural gas in step c)；
● second air-flow of expansion includes natural gas in step d)；And/or
● the product liquid of first refrigerant gas is liquid nitrogen.
In another aspect of the invention, there is provided one kind is used for the first liquefier and the second liquefier integration to produce The method of first liquefied gas and the second liquefied gas.In this embodiment, this method may comprise steps of：A) providing has Using the first liquefier of the first kind of refrigeration cycle of the first refrigerant, wherein first kind of refrigeration cycle is configured to hand in the first heat Refrigeration is provided in parallel operation；B) provide with using second refrigerant the second kind of refrigeration cycle the second liquefier, wherein this second Kind of refrigeration cycle is configured to provide refrigeration in second heat exchanger；C) in the first heat exchanger by with this first refrigeration Circulation carries out heat exchange and cools down the first air-flow to produce the first air-flow of cooling；D) in the second heat exchanger by with this Two kind of refrigeration cycle carry out heat exchange and cool down the second air-flow to produce the second air-flow of cooling；E) make the 3rd flow expansion swollen to produce The 3rd swollen air-flow；And f) in the group being made of the first heat exchanger, the second heat exchanger and combinations thereof The 3rd air-flow of the expansion is heated in heat exchanger to produce the air-flow of heating, wherein except being provided by second kind of refrigeration cycle Outside refrigeration, step f) provides the refrigeration for cooling down second air-flow, wherein except being provided by first kind of refrigeration cycle Outside refrigeration, step f) provides the refrigeration for cooling down first air-flow, and wherein first kind of refrigeration cycle and this second Kind of refrigeration cycle shares a common recycle compressor.
In for the optional embodiment of the first liquefier and the integrated method of the second liquefier：
● first and second kind of refrigeration cycle is nitrogen kind of refrigeration cycle；
● first refrigerant and the second refrigerant have identical composition；
● first air-flow is selected from the group, which is made of the following：Natural gas, ethane, ethene, acetylene, other C3-C6 alkane Hydrocarbon, alkene and alkynes and nitrogen, and wherein first air-flow liquefies during cooling step c)；
● first air-flow is selected from the group that is made of hydrogen and helium, wherein first air-flow not liquid during cooling step c) Change；
● the 3rd air-flow of expansion includes natural gas in step e)；
● by a part for first refrigerant in first kind of refrigeration cycle extract and liquefy produce the first refrigerant of liquid Product, this is introduced wherein the first refrigerant of gaseous state of at least moiety is shone to extract as the first refrigerant of liquid as former state In first kind of refrigeration cycle；And/or
● by a part for the second refrigerant in second kind of refrigeration cycle extract and liquefy produce liquid second refrigerant, Wherein the second refrigerant of at least moiety is shone to extract as liquid second refrigerant and be incorporated into second system as former state In SAPMAC method.
In another aspect of the invention, there is provided one kind is used for liquefaction of nitrogen device and natural gas depressurization integration to produce The method of liquid nitrogen (" LIN ").In this embodiment, this method may comprise steps of：A) providing has nitrogen kind of refrigeration cycle Liquefaction of nitrogen device, the wherein liquefaction of nitrogen device includes nitrogen recycle compressor, heat exchanger and the first turbocharger；b) Nitrogen stream is introduced into the liquefaction of nitrogen device under the conditions of effective for liquefaction nitrogen to produce liquid nitrogen product；C) from first Pressure PHThe source of lower operation extracts natural gas flow；D) natural gas flow is purified in purification unit to produce the natural of purifying Gas；E) natural gas of the purifying is partly cooled down in the heat exchanger；F) this is extracted from the centre portion of the heat exchanger The natural gas of part cooling；G) natural gas that the part cools down is made to press P in being expanded into natural gas expansion turbineMIt is cold to be formed Natural gas flow, wherein presses P in thisMIn less than first pressure PHPressure；And h) in the heat exchanger by with from The nitrogen of the nitrogen kind of refrigeration cycle carries out heat exchange and heats the cold natural gas flow to produce the day of heating from the hot junction of the heat exchanger Right air-flow, wherein step h) provide additional refrigeration to the liquefaction of nitrogen device so that with without step c)-i) method phase Than additional liquid nitrogen can be produced, wherein natural gas expansion turbine driving first gas booster.
In the optional embodiment of integrated method is depressurized for liquefaction of nitrogen device and natural gas flow：
● the first gas booster is configured to compress the natural gas flow or the stream from it；
● the first gas booster is configured to compress stream selected from the group below, which is made of the following：The natural gas flow, The natural gas flow of the purifying, the part cooling natural gas flow, the heating natural gas flow and the nitrogen kind of refrigeration cycle in nitrogen Fluid；
● the purification unit is configured at least remove water from the natural gas flow；
● the nitrogen kind of refrigeration cycle further includes nitrogen feed compressor；
● the liquefaction of nitrogen device further includes subcooler；
● the gas source includes natural gas line；And/or
● the natural gas line has the pressure between 15 and 100 absolute pressures.
In another aspect of the invention, there is provided one kind is used for liquefaction of nitrogen device and natural gas depressurization integration to produce The method of liquid nitrogen (" LIN ").In this embodiment, this method may comprise steps of：A) providing has nitrogen kind of refrigeration cycle Liquefaction of nitrogen device, the wherein liquefaction of nitrogen device includes nitrogen recycle compressor, heat exchanger and at least one turbocharging Device；B) nitrogen stream is introduced under the conditions of effective for liquefaction nitrogen in the liquefaction of nitrogen device to produce liquid nitrogen product；C) from High-voltage power supply recycles natural gas flow, and the wherein natural gas flow is in first pressure；D) make the natural gas flow be expanded into second pressure with The natural gas flow of expansion is produced, the wherein second pressure is less than the pressure of the first pressure；And e) in the heat exchanger The natural gas flow of the expansion is heated to produce the natural gas flow of heating, wherein step e) provides additional system to the liquefaction of nitrogen device It is cold so that compared with without step d) to method e), additional liquid nitrogen can be produced.
Brief description of the drawings
With reference to be described below, claims and drawing, these and other features, aspect and advantage of the invention will become more It is good to understand.It should be noted, however, that attached drawing show only some embodiments of the present invention and therefore be not considered as to this The limitation of invention scope, because the present invention can allow other equivalent embodiments.
Fig. 1 provides the embodiment of the prior art.
Fig. 2 provides the embodiment of the present invention.
Fig. 3 provides the embodiment of the present invention of the production with both LIN and LNG.
Fig. 4 provides an alternative embodiment of the invention of the production with both LIN and LNG.
Fig. 5 provides the embodiment of the present invention with LIN and middle pressure natural gas production.
Embodiment
Although the present invention will be described with reference to some embodiments, it should be understood that, it is not intended to the present invention is limited It is formed on those embodiments.On the contrary, it is intended to cover the spirit of the invention being defined by the appended claims and model can be included in Enclose interior all alternative solutions, modification and equivalent.
In one embodiment, this method can include natural gas depressurization system is integrated with nitrogen kind of refrigeration cycle.One In a embodiment, which is closed-loop refrigeration cycle.In this embodiment, natural gas depressurization substantially provides " certainly By " cooling power, because natural gas will be alternately across valve decompression (that is, general who has surrendered at a temperature of caused natural gas By environment absorb and will not by it is any it is significant in a manner of recover).With the addition of natural gas turbines booster, LNG can be with With significant power save co-production, while it is also possible to reduce the size of nitrogen kind of refrigeration cycle.In another embodiment, may be used also With including purification unit, storage, loading and synergic system.
Reference Fig. 2, shows the process flow chart of the embodiment of the present invention.In fig. 2, high-pressure natural gas 2 is preferably divided into Two parts, a portion liquefies and another part provides and is used to cool down the part with the refrigeration of liquefied natural gas.Natural gas The Part I 102 of stream purifies in the first purification unit 130, wherein it is preferred that removing sour gas, water and mercury.Preferably, day Will be solidified before natural gas liquefaction in right gas or any impurity of damage upstream device in the first purification unit 130 by except Go.Then the Part I 104 of the purifying of caused natural gas flow is extracted and is incorporated into from the first purification unit 130 To liquefy wherein in heat exchanger 40.In wherein natural gas feed contains the embodiment of heavy hydrocarbon, preferably from heat exchanger 40 Centre portion extract natural gas purifying Part I 104 and using gas-liquid separator 5 separate heavy hydrocarbon 8.Alternately, Gas-liquid separator can be replaced with distillation column known in the art or other separators.Instead of weight is collected separately as shown in Figure 1 Hydrocarbon 8, heavy hydrocarbon 8 can be expanded in heat exchanger 40 and then heated.The stream of caused heating can be with other natural gas flows (for example, Part I 146 of cold natural gas flow 144 and LNG) combination in heat exchanger 40.This is advantageously captured to conduct oneself with dignity Some cold energy of hydrocarbon 8, and if the natural gas flow 108 of heating then is used for fuel, it also provides additional energy and is used for The purpose.
The natural gas of vaporization from gas-liquid separator 5 is re-introduced into heat exchanger 40, and wherein it then liquefies To produce LNG 6.In one embodiment, the Part I 146 of LNG can be removed from LNG 6, swollen in the second valve V2 It is swollen, and then heated in heat exchanger 40, additional refrigeration is thus provided, to produce the natural gas flow 108 of heating.Remaining Then part can be expanded across the 3rd valve V3, thus produce low pressure LNG 148.
The refrigeration of system is provided by two sources.First refrigeration source can be via conventional nitrogen kind of refrigeration cycle 50.Nitrogen is existed Compress in nitrogen recycle compressor 10, cooled down in cooler 11, in the booster of the first turbocharger 20 further Compression, cools down in cooler 21, is then further compressed in the booster of the second turbocharger 25, afterwards in cooler Cooled down again in 26.Then the compressed nitrogen caused by cooling in heat exchanger 40, wherein Part I are removed and the Expanded in the turbine of two turbocharger 25, and remainder is removed and swollen in the turbine of the first turbocharger 20 It is swollen.Then the nitrogen stream of caused expansion is incorporated into heat exchanger 40, by the nitrogen of these expansions in the heat exchanger Air-flow is heated via indirect heat exchange is carried out with natural gas and other nitrogen streams.
Second refrigeration source is provided by using the excessive pressure difference of high-pressure natural gas.In this embodiment, natural gas flow Part II 106 is separated from high-pressure natural gas 2, and then in the second purification unit 131 with least water and possible mercury Middle purifying, to produce the Part II 132 of the purifying of natural gas.Although embodiment shown in Figure 2 is individually pure including two Change unit, before natural gas to be divided into two streams, the whole natural gas flow of Economical Purification can be carried out using single purification unit.So And preferably before purification separate stream, because need not be removed for the natural gas (that is, not liquefied part) for providing refrigeration Carbon dioxide, because at a temperature of natural gas turbines outlet stream 144 is in fully heating so that carbon dioxide will not be in this stream Inside freeze.In another embodiment, unit 130 and 131 can be combined into individual unit, and in the middle position of container Moisture free stream (for example, 132) is removed, and by moisture-free and CO2Stream (for example, 104) from container and feed position Opposite end is put to remove.
Then the Part II 132 of the purifying of natural gas is compressed in the booster of natural gas turbines booster 120, Cooled down in cooler 140 to produce the natural gas flow 142 of compression.Then can be by the natural gas flow 142 of compression in heat exchanger Partly cool down in 40, expanded afterwards in the turbine of natural gas turbines booster 120 to form cold natural gas flow 144.It can replace Dai Di, in unshowned embodiment, natural gas flow 142 can be transmitted directly to before cooling in natural gas turbines 120 into Row expansion.This can help to limit 144 temperature to avoid heavy hydrocarbon condensation and possible solidification.Then by cold natural gas flow 144 It is re-introduced into heat exchanger 40, wherein the cold natural gas flow is heated by indirect heat exchange and from the heat of the heat exchanger Hold and be collected as the natural gas flow 108 of heating.In one embodiment, cold natural gas flow 144 can with heavy hydrocarbon 8 and optionally The Part I 146 of ground LNG combines in heat exchanger, or these different streams can individually heat simultaneously in heat exchanger Combined after its heating.
The booster of natural gas turbines booster 120 can be located at many different positions, this depend on gas source and Returning pressure.For example, it can be located at：If 1) feed pressure and/or returning pressure are low, at NG streams to be expanded (Fig. 2)；2) At the total natural gas feed stream being divided into before stream to be expanded and stream to be liquefied (Fig. 3), or 3) in high natural gas feed pressure In the case of power and high natural returning pressure, (do not show in the discharge of the turbine at the hot junction of exchanger (for example, stream 108) place Go out), if or 4) feed pressure is low, (not shown) on natural gas flow to be liquefied (for example, stream 104).Alternately, turbine can For driving generator or being consumed by oil brake (not shown).
The comparison of embodiment shown in Fig. 1 and 2 can be found in following Table I：
Table I：The comparison of the energy requirement of Fig. 1 and Fig. 2
In the device shown in Fig. 2, produce the power needed for the LNG of 342mtd and be reduced to about 4158kW, it means that this The specific power of kind device is about 292kWh/mt.Therefore, this represent power demand to decline about 42%.
On Fig. 3, the common technique for producing liquid nitrogen and the embodiment of LNG is combined with natural gas depressurization using nitrogen kind of refrigeration cycle Flow chart.In figure 3, natural gas can be obtained from gas source, and high pressure day is compressed to produce in natural gas booster 101 Right gas 2.High-pressure natural gas 2 is preferably divided into two parts, and a portion liquefies and another part provides and is used for the day that cools down and liquefy A part for the refrigeration of right gas.The Part I 102 of natural gas flow purifies in the first purification unit 130, wherein it is preferred that removing Sour gas, water and mercury.Preferably, any impurity that will be damaged or solidify before natural gas liquefaction in natural gas is first It is removed in purification unit 130.Then by the Part I 104 of the purifying of caused natural gas flow from the first purification unit Extract and be incorporated into heat exchanger 40 to liquefy wherein in 130.Natural gas feed contains the embodiment of heavy hydrocarbon wherein In, the Part I 104 of the purifying of natural gas is preferably extracted from the centre portion of heat exchanger 40 and uses gas-liquid separator 5 Separate heavy hydrocarbon 8.Alternately, gas-liquid separator can be replaced with distillation column known in the art or other separators.Instead of Heavy hydrocarbon 8 is collected separately as shown in Figure 1, heavy hydrocarbon 8 can be expanded in heat exchanger 40 and then heated.Caused heating stream It can be combined with cold natural gas flow 144 in heat exchanger 40.This advantageously captures some cold energy from heavy hydrocarbon 8, and If the natural gas flow 108 of heating then is used for fuel, it also provides additional energy for the purpose.
The natural gas of vaporization from gas-liquid separator 5 is re-introduced into heat exchanger 40, and wherein it then liquefies To produce LNG 6.Although not specifically illustrating in figure 3, in Fig. 2, in one embodiment, the Part I 146 of LNG can be from Remove in LNG 6, expanded in the second valve V2, and then heated in heat exchanger 40, thus additional refrigeration is provided, To produce the natural gas flow 108 of heating.Then remainder can be expanded across the 3rd valve V3, thus produce the second of LNG Part 148.In the embodiment shown in fig. 3, all LNG 6 expand in valve V3 and are used as product.
The refrigeration of system is provided by two sources.First refrigeration source can be via conventional nitrogen kind of refrigeration cycle 50.Nitrogen is existed Compress in nitrogen recycle compressor 10, cooled down in cooler 11, in the booster of the first turbocharger 20 further Compression, cools down in cooler 21, is then further compressed in the booster of the second turbocharger 25, afterwards in cooler Cooled down again in 26.Then the compressed nitrogen caused by cooling in heat exchanger 40, wherein Part I are removed and the Expanded in the turbine of two turbocharger 25, Part II is removed and is expanded in the turbine of the first turbocharger 20.So The nitrogen stream of caused expansion is incorporated into heat exchanger 40 afterwards, the nitrogen by these expansions in the heat exchanger flows through Heated by carrying out indirect heat exchange with natural gas and other nitrogen streams.
Second refrigeration source is provided by using the excessive pressure difference of high-pressure natural gas.In this embodiment, natural gas flow Part II 106 is separated from high-pressure natural gas 2, and then in the second purification unit 131 with least water and preferred mercury Middle purifying, to produce the Part II 132 of the purifying of natural gas.Although the embodiment shown in Fig. 3 is individually pure including two Change unit, before natural gas to be divided into two streams, the whole natural gas flow of Economical Purification can be carried out using single purification unit.So And preferably before purification separate stream, because need not be removed for the natural gas (that is, not liquefied part) for providing refrigeration Carbon dioxide, because at a temperature of natural gas turbines outlet stream 144 is in fully heating so that carbon dioxide will not be in this stream Inside freeze.In another embodiment, unit 130 and 131 can be combined into individual unit, and in the middle position of container Moisture free stream (for example, 132) is removed, and by moisture-free and CO2Stream (for example, 104) from container and feed position Opposite end is put to remove.
Then the Part II 132 of the purifying of natural gas can partly be cooled down in heat exchanger 40, afterwards in day Expanded in the turbine 121 of right air turbine booster 120 to form cold natural gas flow 144.Alternately, in unshowned embodiment In, the Part II 132 of the purifying of natural gas flow can be transmitted directly to carry out in natural gas turbines 121 swollen before cooling It is swollen.This can help to limit 144 temperature to avoid heavy hydrocarbon condensation and possible solidification.Then by cold natural gas flow 144 again It is incorporated into heat exchanger 40, wherein the cold natural gas flow is heated by indirect heat exchange and is made from the hot junction of the heat exchanger It is collected for the natural gas flow 108 of heating.In one embodiment, cold natural gas flow 144 can be with heavy hydrocarbon 8 in heat exchanger Combination, or these different streams can individually be heated in heat exchanger and combined after its heating.
The booster 101 of natural gas turbines booster 120 can be located at many different positions, this depends on gas source And returning pressure.For example, it can be located at：If 1) feed pressure and/or returning pressure are low, at NG streams to be expanded (Fig. 2)； 2) at the total natural gas feed stream being divided into before stream to be expanded and stream to be liquefied (Fig. 3), or 3) in high natural gas feed In the case of pressure and high natural returning pressure, (do not show in the discharge of the turbine at the hot junction of exchanger (for example, stream 108) place Go out), if or 4) feed pressure is low, (not shown) on stream to be liquefied (for example, stream 104).Alternately, turbine can be used for driving Dynamic generator is consumed by oil brake (not shown).
The main distinction between the embodiment of Fig. 2 and the embodiment of Fig. 3 be in figure 3, using low-pressure gaseous nitrogen as into Material is incorporated into nitrogen kind of refrigeration cycle and produces LIN and LNG jointly.In a specific embodiment, gaseous nitrogen (" GAN ") is introduced Into nitrogen compressor 15 and by its compression, cool down and be then added in kind of refrigeration cycle in cooler 16 afterwards.Ability Domain skilled artisan will realize that, nitrogen compressor 15 can be it is optional because its use can depend on GAN feed The pressure of stream.In another embodiment, the Part III of the nitrogen of cooling is removed from heat exchanger 40, in nitrogen subcooler It is subcooled in 45, and is expanded across valve V4, is incorporated into afterwards in nitrogen liquid/gas separator 55.Nitrogen steam 57 is separated from Nitrogen Headspace The top of device 55 extracts and is then heated in heat exchanger 40, wherein by it before kind of refrigeration cycle is rejoined again Recompressed by nitrogen compressor 15.Liquid nitrogen is extracted from the bottom of nitrogen liquid/gas separator 55, and preferably by a part Vaporized in 51 feeding subcoolers 45, and another part 52 is sent into liquid nitrogen storage tank (not shown).
Therefore, Fig. 3 provides the embodiment of combination LIN+LNG+ natural gas depressurizations.As it was previously stated, nitrogen kind of refrigeration cycle includes Recycle compressor and at least one turbocharger.However, because it produces LIN (for example, nitrogen molecular is removed from circuit), So it further includes the step of gaseous nitrogen charging is added into system.In the embodiment shown in fig. 3, gaseous nitrogen composition is in low Pressure, and therefore it further includes nitrogen feed compressor and provides the subcooler of liquid nitrogen product.As in other embodiments that Sample, natural gas supply separate between stream to be liquefied and the stream of low pressure to be expanded back to.As previously noted, natural gas booster 101 can be located at different positions, this depends on the flow-rate ratio and pressure and used decompressed pressure of natural gas feed.
With reference to figure 4, the technique for showing the embodiment of the sectoral integration with liquefaction of nitrogen device Yu natural gas liquefaction device Flow chart.In Fig. 4, natural gas can be obtained from gas source, and high pressure day is compressed to produce in natural gas booster 101 Right gas 2.High-pressure natural gas 2 is preferably divided into two parts, and a portion liquefies and another part is provided for liquefied natural gas A part for refrigeration.The Part I 102 of natural gas flow purifies in the first purification unit 130, wherein it is preferred that removing sour gas Body, water and mercury.Preferably, it is before natural gas liquefaction that any impurity for damaging equipment or solidification is pure first in natural gas Change and be removed in unit 130.Then by the Part I 104 of the purifying of caused natural gas flow from the first purification unit 130 In extract and be incorporated into heat exchanger 440 to liquefy wherein.In wherein natural gas feed contains the embodiment of heavy hydrocarbon, It is preferred that first of the purifying of natural gas is extracted from the centre portion of heat exchanger 440 or before exchanger 440 is entered Divide 104 and using gas-liquid separator 5 or distillation post separation heavy hydrocarbon 8.In one embodiment, heavy hydrocarbon 8 can be in heat exchanger 440 It is middle to expand and then heat.The stream of caused heating can be handed over other natural gas flows (for example, cold natural gas flow 144) in heat Combination in parallel operation 440.This advantageously captures some cold energy from heavy hydrocarbon 8, and if then by the natural gas flow of heating 108 are used for fuel, it also provides additional energy for the purpose.The natural gas of vaporization from gas-liquid separator 5 is by again It is incorporated into heat exchanger 440, wherein it then liquefies to produce LNG 6.
The refrigeration of system can be provided by three sources：First nitrogen kind of refrigeration cycle 50, the second nitrogen kind of refrigeration cycle 450 and pass through height Press the expansion of natural gas.In the first nitrogen kind of refrigeration cycle 50, the first nitrogen kind of refrigeration cycle 50 and the second nitrogen kind of refrigeration cycle 450 will be come from Nitrogen compressed in shared nitrogen recycle compressor 410, and cooled down in cooler 411.Then by caused pressure Contracting nitrogen is divided into two streams, and Part I enters the first nitrogen kind of refrigeration cycle 50 and Part II enters the second nitrogen kind of refrigeration cycle 450。
On the first nitrogen kind of refrigeration cycle 50, nitrogen can further be pressed in the booster of the first turbocharger 20 Contracting, cools down in cooler 21, is further compressed in the booster of the second turbocharger 25, in cooler 26 again afterwards Secondary cooling.Then compressed nitrogen, wherein Part I are removed and in the second turbines caused by cooling in heat exchanger 40 Expanded in the turbine of booster 25, Part II is removed and is expanded in the turbine of the first turbocharger 20.Then by institute The nitrogen stream of the expansion of generation is incorporated into heat exchanger 40, in the heat exchanger by these expansion nitrogen stream via with day Right gas and other nitrogen streams carry out indirect heat exchange and heat, and are then returned to shared nitrogen recycle compressor 410 In.
As in figure 3, the embodiment of Fig. 4 further includes the low-pressure gaseous nitrogen introduced as charging and co-production LIN.Will Gaseous nitrogen (GAN) is incorporated into nitrogen compressor 15 and by its compression, cools down and be then added in cooler 16 afterwards In kind of refrigeration cycle.Those of ordinary skill in the art are it will be recognized that nitrogen compressor 15 can be optional, because its use can With the pressure depending on GAN feeding flows.In addition, the remainder of compressed nitrogen is removed from heat exchanger 40, it is subcooled in nitrogen It is subcooled in device 45, and is expanded across valve V4, is incorporated into afterwards in nitrogen liquid/gas separator 55.Nitrogen steam 57 is divided from Nitrogen Headspace Top from device 55 extracts and is then heated in heat exchanger 40, wherein will before kind of refrigeration cycle is rejoined again It is recompressed by nitrogen compressor 15.Liquid nitrogen is extracted from the bottom of nitrogen liquid/gas separator 55, is then divided into Part I 51 (vaporization is to provide the heat exchange for LIN supercoolings in subcooler 45) and Part II 52 are (as being preferably sent to storage tank (not Show) LIN products).
Second refrigeration source can be the shared cooler 411 and such as the by shared nitrogen recycle compressor 410 The second of the non-common equipment such as three turbocharger 420, cooler 421, the 4th turbocharger 425 and cooler 426 composition Nitrogen kind of refrigeration cycle 450.
3rd refrigeration source is provided by using the available excessive pressure difference of high-pressure natural gas.In this embodiment, natural gas The Part II 106 of stream is separated from high-pressure natural gas 2, and then in the second purification unit with least water and preferred mercury Purified in 131, to produce the Part II 132 of the purifying of natural gas.Although the embodiment shown in Fig. 4 includes two individually Purification unit, before natural gas to be divided into two streams, can carry out the whole natural gas flow of Economical Purification using single purification unit. It is preferable, however, that stream is separated before purification, because need not be removed for the natural gas (that is, not liquefied part) for providing refrigeration Carbon dioxide is removed, because at a temperature of natural gas turbines outlet stream 144 is in fully heating so that carbon dioxide will not be at this Freeze in stream.Alternately, unit 130 and 131 can be combined into individual unit so that be removed not in the middle position of container The stream 132 of moisture content, and by moisture-free and CO2Stream 104 removed from the container end opposite with 2 positions of charging.
The Part II 132 of the purifying of natural gas can partly be cooled down in heat exchanger 440, afterwards in natural gas Expanded in turbine 121 to form cold natural gas flow 144.Alternately, will can be sent to before stream 132 in a heat exchanger cooling Turbine 121 is expanded, with due to CO2Freeze or heavy hydrocarbon condenses and limits 144 temperature.Then by cold natural gas flow 144 again It is secondary to be incorporated into heat exchanger 440, wherein the cold natural gas flow is heated by indirect heat exchange and from the heat of the heat exchanger Hold and be collected as the natural gas flow 108 of heating.In one embodiment, cold natural gas flow 144 can be with heavy hydrocarbon 8 in heat exchange Combination in device, or the two streams can individually be heated in heat exchanger and combined after its heating.
The booster 101 of natural gas turbines booster 120 can be located at many different positions, this depends on gas source And returning pressure.For example, it can be located at：If 1) feed pressure and/or returning pressure are low, at NG streams to be expanded (Fig. 2)； 2) at the total natural gas feed stream being divided into before stream to be expanded and stream to be liquefied (Fig. 3), or 3) in high natural gas feed In the case of pressure and high natural returning pressure, (do not show in the discharge of the turbine at the hot junction of exchanger (for example, 108) place Go out), if or 4) feed pressure is low, (not shown) on stream to be liquefied (for example, 104).Alternately, turbine can be used for driving Generator is consumed by oil brake (not shown).
As indicated above, the embodiment of Fig. 4 preferably includes to share a common nitrogen with the second nitrogen kind of refrigeration cycle 450 The free-standing liquefaction of nitrogen device 350 of recycle compressor (for example, 410).Therefore, such embodiment advantageously can both have There is liquefaction of nitrogen unit to produce LIN and LNG at the position with gas inlet again.
Compared with the embodiment shown in Fig. 3, the embodiment of Fig. 4 is improved with 12% efficiency, mainly due to additional Turbocharger, these turbocharger can be positioned at the temperature in circulation to independently optimize LNG and LIN groups.
In addition, compared with independent liquefaction of nitrogen device adds independent LNG plant, because the embodiment effectively eliminates one A recycle compressor (the typically maximum fund cost equipment of system), so shared recycle compressor 410 provides Lower capital cost.In addition, compared with two small machines, due to single heavy-duty machines, there are small efficiency raising. Similarly as previously indicated, the position for the booster of natural gas depressurization can become with gas source and decompressed pressure Change.
The comparison of embodiment shown in Fig. 1-4 can be found in following Table II.
Table II：The correction data of Fig. 1-4
In optional embodiment, the 4th air-flow 351 can be cooled and/or liquefy cold to produce in heat exchanger 40 But/liquefied 4th air-flow 352.In one embodiment, the 4th air-flow 351 is selected from the group, which is made of the following：My god Right gas；Ethane；Ethene；Acetylene；C3-C6Alkane, alkene and alkynes；Nitrogen；Hydrogen；And helium.Air-flow 351 is hydrogen wherein Or in the embodiment of helium, air-flow 352 is not preferably liquefied.Otherwise, cooling stream 352 is preferably liquefied.Advantageously, this Optional embodiment allows the single gas of three kinds of liquefaction (for example, stream 52,352 and 6).
Embodiment shown in Fig. 3 and Fig. 4 is preferably placed at big constant de-pressurised natural gas stream (for example, cogeneration of heat and power list Member or steam methane reformer facility) and source nitrogen (for example, close to air gas separation unit " ASU " or nitrogen pipeline) industry Place nearby, on industrial sites or close to the industrial sites.Nitrogen is usually obtainable near ASU, because they are usual It is designed to O2Production.Nitrogen can be extracted in ASU chilldown systems with low cost.
Embodiment shown in Fig. 4 includes the specific embodiment of production LNG and LIN, however, the present invention is not limited thereto.On the contrary, The embodiment of the present invention can include making first gas and second gas liquefy by using two kind of refrigeration cycle, wherein this two A kind of refrigeration cycle shares a common recycle compressor.In a preferred embodiment, kind of refrigeration cycle is nitrogen kind of refrigeration cycle. In one embodiment, two liquefiers can each produce LIN or LNG or liquified hydrogen or liquid helium or other any kind of industry Gas.In another embodiment, any one in liquefier or both can have be configured to make higher pressure gas source swollen Swollen expansion gear.
The embodiment of the present invention can have a wide range of applications in the industry.For example, the embodiment of the present invention can include Identify the liquefaction system underused, and then nearby increase the second liquefier (for example, LNG liquefiers).Original liquid The recycle compressor that changing device can somewhat be modified for allowing to underuse before it provides for two kind of refrigeration cycle Compression.This allows new liquefier to produce its liquid in a manner of more efficient.In another embodiment, the second liquefaction unit is excellent Selection of land is located near high pressure and low pressure pipeline network (for example, natural gas line) so that the system can use and come from natural gas The refrigeration of expansion.
In another embodiment, two new liquefiers can be built to meet the market demand.For example, the first liquefier can To be liquefaction of nitrogen unit and the second liquefier can be natural gas liquefaction unit, the two uses nitrogen kind of refrigeration cycle.May Economically advantageously at least one in liquefier is standardized equipment (for example, the mould that can be designed and produced in bulk Block type design).In many cases, the design capacity of standardized equipment is more than the capacity needed for this concrete application.Similar Concept can be adapted for the repositioning of existing liquefier.Therefore, the second liquefier can be built so that its kind of refrigeration cycle use with The identical recycle compressor of first liquefier.It is also common for such liquefaction device to be located near industrial area, therefore benefits from Extensive natural gas line network.As described herein, one or two liquefier will benefit from increasing into each nitrogen kind of refrigeration cycle Add natural gas swell refrigeration.
Similarly, if standardized equipment is undersized for application-specific (for example, production liquid nitrogen), the can be designed Two liquefaction units make up difference.In this embodiment, the second liquefaction unit may be configured to produce liquid nitrogen product and Both LNG products.
When natural gas turbines drive generator without extracting the cooling power expanded, in fact it could happen that operation problem.In addition, In some cases, the flow of natural gas and pressure may be fluctuated often.Since electric system is not always able to receive to be produced The problem of raw slave generator is sent to the power fluctuation of power transmission network, this may result in the fluctuation on the energy of generation.It is similar Ground, the caused cold fluctuation as caused by expanding natural gas can produce other utility fluctuations.
In certain embodiments of the present invention, above-mentioned the problem of referring to, can be subtracted by using LNG and/or LIN storage tanks Gently, because storage tank provides buffering for the fluctuation of refrigeration balance.For example, the minor fluctuations of natural gas condition can be by adjusting nitrogen system The amount of the load of SAPMAC method and liquefied LNG and/or LIN solves.By stopping liquefier and can be with by tank Liquid level compensator Solve big or long-term fluctuation.In addition, allow high-pressure natural gas by adjusting by-passing valve around liquefier and be directly entered MP GAN stream (not shown) can solve significant short-term fluctuation.In another embodiment, this method can include monitoring day The various process conditions of right source of the gas and/or the stream in gas source downstream (for example, pressure, flow, gas composition etc.).Based on these The process condition of monitoring, can adjust each set point with further optimization system.For example, the set point that can be adjusted can wrap The expansion ratio of different turbines is included, together with the flow of not cocurrent flow from beginning to end.In one embodiment, bypassed by adjusting natural gas Valve and/or turbine inlet control valve, can be by the flow of natural gas turbines and the setpoint control of inlet pressure in liquefaction device Acceptable range of operation in.In one embodiment, this method can include central process controller, the central process control Device processed is configured to receive the process conditions of different monitorings and is then based on monitored process conditions to determine whether to answer The selected set point of the adjusting.Monitoring device can be communicated by all known methods with controller, for example, wirelessly and Via both electrical communications.
Fig. 5 provides process flow chart, and wherein liquid nitrogen production is supplemented with the refrigeration from natural gas depressurization.Subtracted by natural gas The additional-energy that pressure provides reduces the power and size of the nitrogen kind of refrigeration cycle of fixed LIN production, this is depended on can be from natural The amount (that is, the flow and pressure ratio of NG decompressions) of the energy removed in gas decompression.
In such embodiment, system is preferably close to source nitrogen (for example, with available nitrogen production ASU, or other small, dedicated nitrogen gas generators, or nitrogen pipeline) and the suitable pressurized natural gas source depressurized.Although it will be appreciated that Be that gas discharge and pressure can change, but liquefier can be by producing LIN and/or work(from nitrogen kind of refrigeration cycle Rate is adjusted accordingly to adapt to some of these changes.
There is method shown in Fig. 5 one to be used for for the natural gas turbines booster of the heated zones of exchanger and one The nitrogen turbine booster of cold section.However, in order to improve efficiency and flexibility, can wrap in certain embodiments of the present invention Include additional heating turbocharger (as shown in Figure 2).
On purifying, water should be removed, and depending on natural gas composition, pressure and the temperature before natural gas expansion Degree, can equally remove sour gas (such as CO from natural gas2) and other impurity for freezing at a lower temperature.Natural gas exists It can be cooled before expansion and about -60 DEG C to -100 DEG C of temperature can be reached before heat exchanger is entered, be weighed It is new to heat and return to low-pressure header.Due to CO2It can only freeze at a lower temperature, so need not be removed from the stream of expansion CO2。
It is directed at due to liquefier in the industrial plants with constant natural gas depressurization, source nitrogen etc., these facilities lead to Often there is the impurity of much less in feed natural gas.Such as in that region without using adding smelly the mercaptan of sulfur-bearing (add). Therefore, compared with the similar units installed in non-industry spot, purification system can be simplified.
Those of ordinary skill in the art are it will be recognized that other kinds of kind of refrigeration cycle can be used.Therefore, it is of the invention Embodiment is not limited to the specific kind of refrigeration cycle for showing and describing in detail specifications and attached drawing.In addition, although in attached drawing In show and embodiment discussed herein typically illustrates natural gas expansion turbine and may be coupled to natural gas booster, but It is that certain embodiments of the present invention is not intended to and is so limited.On the contrary, in certain embodiments of the present invention, natural gas expansion whirlpool Wheel 121 can drive the booster in one of kind of refrigeration cycle (such as nitrogen kind of refrigeration cycle).In this embodiment, booster It may be configured to the cryogenic fluid (for example, nitrogen) in compression kind of refrigeration cycle.
Although having been combined its specific embodiment, the invention has been described, it is evident that in view of many alternatives of preceding description Case, modification and change will be apparent for those skilled in the art.Therefore, it, which is intended to include, such as falls into appended claims Spirit and broad scope in all such alternative solutions, modification and change.The present invention can be wanted suitably comprising disclosed Element, be made of disclosed key element or be substantially made of disclosed key element, and can be there is no the key element not disclosed Lower practice.In addition, if in the presence of the language for referring to order, such as first and second, it should exist on illustrative sense and not Understood in restrictive, sense.For example, it will also be recognized by those skilled in the art that some steps can be combined to single In step.
Singulative "/kind " (a/an) and " being somebody's turn to do (the) " include plural referents, unless context is expressly otherwise Point out.
" including (comprising) " in claim is open transitional term, its refer to it is later determined that right will It is that (that is, other anythings can additionally be included and be maintained at the scope of "comprising" without exclusive inventory to seek key element It is interior).Unless otherwise indicated herein, otherwise "comprising" as used herein can by be more confined from transitional term " mainly by ... Composition " and " consist of " replace.
" provide (providing) " in claim be defined as confession under directions to, supply, make to obtain or prepare certain Thing.The step can be carried out by any actor under the representation language in there is no this opposite claim.
It is optional or optionally mean that the event then described or situation may occur or may not occur.This explanation includes The wherein example that the event or situation occur and the example that wherein event or situation do not occur.
It can be expressed as from about occurrence in this scope, and/or to about another occurrence.When such a scope of statement When, it should be understood that another embodiment is from an occurrence and/or to another occurrence, together with the scope Interior all combinations.
Each be attached to hereby by quoting with its full text in the application in this definite all bibliography, and be for Specific information, each bibliography is cited is exactly for the specifying information.

Claims (77)

1. one kind is used for the method for producing liquefied natural gas (" LNG "), this method comprises the following steps：
A) nitrogen kind of refrigeration cycle (50) is provided, the wherein nitrogen kind of refrigeration cycle is configured to provide refrigeration in heat exchanger (40)；
B) the first natural gas flow of purifying (102) is to remove first group of impurity in the first purification unit (130), so as to produce purifying The first natural gas flow (104)；
C) in the heat exchanger using the refrigeration from the nitrogen kind of refrigeration cycle come first natural gas flow (104) that cools down and liquefy To produce LNG stream (6), wherein first natural gas flow has LNG refrigeration demands, and wherein the LNG stream is in first pressure PHLower liquid Change；
D) the second natural gas flow of purifying (106) is to remove second group of impurity in the second purification unit (131), so as to produce purifying The second natural gas flow (132)；
E) second natural gas flow (142) is partly cooled down in the heat exchanger；
F) the second natural gas flow of part cooling is extracted from the centre portion of the heat exchanger；
G) the second natural gas flow that the part cools down is made to be expanded into middle pressure P in natural gas expansion turbine (120)MTo form cold day Right air-flow (144), wherein presses P in thisMIn less than first pressure PHPressure；And
H) the cold natural gas flow is heated with heat friendship by carrying out heat exchange with first natural gas flow in the heat exchanger The hot junction of parallel operation produces the natural gas flow (108) of heating,
Wherein the natural gas expansion turbine drives the first booster,
Wherein the LNG refrigeration demands are provided by the combination from the nitrogen kind of refrigeration cycle (50) and the refrigeration of step h).
2. the method as described in claim 1, wherein first booster be configured to compress second natural gas flow (106) or Person derives from the stream of second natural gas flow.
3. the method as described in claim 1, wherein first booster are configured to compress stream selected from the group below, the group by with Lower every composition：First natural gas flow, this first purifying natural gas flow, second natural gas flow, second day of the purifying Right air-flow, the natural gas flow of part cooling, the heating natural gas flow and the nitrogen kind of refrigeration cycle in nitrogen fluid.
4. the method as described in claim 1, wherein first group of impurity is in first pressure PHIt is lower to have at or greater than methane Condensing temperature solidification point.
5. the method as described in claim 1, wherein second group of impurity include water.
6. the method as described in claim 1, wherein the nitrogen kind of refrigeration cycle include recycle compressor (10), turbine (20,25), increase Depressor (20,25) and multiple coolers (11,21,26), the wherein turbine and booster be configured so that the turbine by with It is set to and provides power for the booster.
7. the method as described in claim 1, wherein first natural gas flow and second natural gas flow are from same natural Source of the gas (2).
8. the method for claim 7, wherein the gas source is with the natural of the pressure between 15 and 100 absolute pressures Feed channel.
9. the method as described in claim 1, wherein first natural gas flow come from the first gas source, and this is second natural Air-flow comes from the second gas source, and wherein first gas source and second gas source is different sources.
10. method as claimed in claim 9, wherein first gas source include natural gas line.
11. method as claimed in claim 10, the wherein natural gas line have the pressure between 15 and 100 absolute pressures.
12. the method as described in claim 1, wherein first purification unit and second purification unit are same units.
13. the method as described in claim 1, wherein first purification unit and second purification unit are separated units, Wherein first purification unit is configured at least remove water and carbon dioxide, and wherein second purification unit is configured to At least remove water.
14. one kind is used for the method for producing liquefied natural gas (" LNG "), this method comprises the following steps：
Nitrogen kind of refrigeration cycle (50) a) is provided；
B) first is cooled down and liquefies by carrying out heat exchange with the nitrogen from the nitrogen kind of refrigeration cycle (50) in a heat exchanger To produce LNG stream (6), the wherein LNG stream liquefies natural gas flow (104) at the first pressure；
C) the second natural gas flow (132) is made to be expanded into second pressure to produce the natural gas flow of expansion；And
D) natural gas flow (144) of the expansion is heated in the heat exchanger to produce the natural gas flow (108) of heating,
Wherein step d) provides a part for the refrigeration for first natural gas flow that cools down and liquefy.
15. method as claimed in claim 14, wherein first natural gas flow come from the first gas source, and this second day Right air-flow comes from the second gas source, and wherein first gas source and second gas source is different sources.
16. method as claimed in claim 14, wherein liquefied first gas source is in the expansion in step b) Natural gas flow, the wherein first pressure are roughly the same with the second pressure.
17. one kind is used for the method for producing liquefied natural gas (" LNG "), this method comprises the following steps：
A) high-pressure natural gas stream is provided；
B) the high-pressure natural gas stream is divided into Part I and Part II；
C) Part I of cooling and the high-pressure natural gas stream that liquefies is to produce LNG stream；
D) the first refrigerating part is provided via nitrogen kind of refrigeration cycle, the wherein nitrogen kind of refrigeration cycle includes recycle compressor, turbine, supercharging It is dynamic that device and multiple coolers, the wherein turbine and booster are configured so that the turbine is configured to booster offer Power；
E) the second refrigerating part is provided by expanding the Part II of the high-pressure natural gas；And
F) using first refrigerating part and second refrigerating part come realize the high-pressure natural gas stream in step c) this The cooling and liquefaction of a part.
18. one kind is used for the method for producing liquefied natural gas (" LNG ") and liquid nitrogen (" LIN "), this method comprises the following steps：
A) nitrogen kind of refrigeration cycle is provided, the wherein nitrogen kind of refrigeration cycle is configured to provide refrigeration in heat exchanger, wherein the nitrogen system A part for nitrogen in SAPMAC method, which is extracted and liquefies, produces liquid nitrogen product, wherein the gaseous nitrogen of at least moiety is shone Extract and be incorporated into as former state in the nitrogen kind of refrigeration cycle；
B) the first natural gas flow is purified in the first purification unit to remove first group of impurity, so that produce purifying first is natural Air-flow；
C) in the heat exchanger using the refrigeration from the nitrogen kind of refrigeration cycle first natural gas flow is cooled down and liquefied to produce Raw LNG stream, wherein first natural gas flow have LNG refrigeration demands, and wherein the LNG stream is in first pressure PHLower liquefaction；
D) the second natural gas flow is purified in the second purification unit to remove second group of impurity, so that produce purifying second is natural Air-flow；
E) second natural gas flow is partly cooled down in the heat exchanger；
F) the second natural gas flow of part cooling is extracted from the centre portion of the heat exchanger；
G) the second natural gas flow that the part cools down is made to press P in being expanded into natural gas expansion turbineMTo form cold natural gas Stream, wherein presses P in thisMIn less than first pressure PHPressure；And
H) the cold natural gas flow is heated with heat friendship by carrying out heat exchange with first natural gas flow in the heat exchanger The hot junction of parallel operation produces the natural gas flow of heating,
Wherein the natural gas expansion turbine drives the first booster,
Wherein the LNG refrigeration demands are provided by the combination from the nitrogen kind of refrigeration cycle and the refrigeration of step h).
19. method as claimed in claim 18, wherein first booster be configured to compress second natural gas flow or From the stream of second natural gas flow.
20. method as claimed in claim 18, wherein first booster are configured to compress stream selected from the group below, the group by The following forms：First natural gas flow, the first natural gas flow of the purifying, second natural gas flow, the second of the purifying Natural gas flow, the part cooling natural gas flow, the heating natural gas flow and the nitrogen kind of refrigeration cycle in nitrogen fluid.
21. method as claimed in claim 18, the wherein liquid nitrogen product have LIN refrigeration demands, wherein the LIN refrigeration demands There is provided by the combination from the nitrogen kind of refrigeration cycle and the refrigeration of step h).
22. method as claimed in claim 18, wherein first group of impurity is in first pressure PHIt is lower to have at or greater than first The solidification point of the condensing temperature of alkane.
23. method as claimed in claim 18, wherein second group of impurity include water.
24. method as claimed in claim 18, wherein the nitrogen kind of refrigeration cycle include recycle compressor, turbine, booster and more A cooler, the wherein turbine and booster are configured so that the turbine is configured to the booster and provides power.
25. method as claimed in claim 24, wherein the nitrogen kind of refrigeration cycle further include nitrogen feed compressor.
26. method as claimed in claim 18, wherein first natural gas flow and second natural gas flow come from same day Right source of the gas.
27. method as claimed in claim 26, the wherein gas source are the days with the pressure between 15 and 100 absolute pressures Right feed channel.
28. method as claimed in claim 18, wherein first natural gas flow come from the first gas source, and this second day Right air-flow comes from the second gas source, and wherein first gas source and second gas source is different sources.
29. method as claimed in claim 28, wherein first gas source include natural gas line.
30. method as claimed in claim 29, the wherein natural gas line have the pressure between 15 and 100 absolute pressures.
31. method as claimed in claim 18, wherein first purification unit and second purification unit are same units.
32. method as claimed in claim 18, wherein first purification unit and second purification unit are separated units, Wherein first purification unit is configured at least remove water and carbon dioxide, and wherein second purification unit is configured to At least remove water.
33. method as claimed in claim 18, wherein the liquefaction of nitrogen device further include subcooler.
34. one kind is used for the method for producing liquefied natural gas (" LNG ") and liquid nitrogen (" LIN "), this method comprises the following steps：
A) nitrogen kind of refrigeration cycle is provided, the wherein nitrogen kind of refrigeration cycle is configured to provide refrigeration in heat exchanger, wherein the nitrogen system A part for nitrogen in SAPMAC method, which is extracted and liquefies, produces liquid nitrogen product, wherein the gaseous nitrogen of at least moiety is shone Extract and be incorporated into as former state in the nitrogen kind of refrigeration cycle；
B) it is first natural to cool down and liquefy by carrying out heat exchange with the nitrogen from the nitrogen kind of refrigeration cycle in a heat exchanger Air-flow is to produce LNG stream, and wherein the LNG stream liquefies at the first pressure；
C) the second natural gas flow is made to be expanded into second pressure to produce the natural gas flow of expansion；And
D) natural gas flow of the expansion is heated in the heat exchanger to produce the natural gas flow of heating,
Wherein step d) provides a part for the refrigeration for first natural gas flow that cools down and liquefy.
35. method as claimed in claim 34, wherein first natural gas flow come from the first gas source, and this second day Right air-flow comes from the second gas source, and wherein first gas source and second gas source is different sources.
36. method as claimed in claim 34, the wherein liquid nitrogen product have LIN refrigeration demands, wherein the LIN refrigeration demands There is provided by the combination from the nitrogen kind of refrigeration cycle and the refrigeration of step d).
37. method as claimed in claim 34, wherein liquefied first gas source is in the expansion in step b) Natural gas flow, the wherein first pressure are roughly the same with the second pressure.
38. one kind is used for the method for producing liquefied natural gas (" LNG ") and liquid nitrogen (" LIN "), this method comprises the following steps：
A) nitrogen kind of refrigeration cycle is provided, the wherein nitrogen kind of refrigeration cycle includes recycle compressor, turbine, booster and multiple coolings Device, the wherein turbine and booster are configured so that the turbine is configured to the booster and provides power, wherein the nitrogen system A part for nitrogen in SAPMAC method, which is extracted and liquefies, produces liquid nitrogen product, wherein the gaseous nitrogen of at least moiety is shone Extract and be incorporated into as former state in the nitrogen kind of refrigeration cycle；
B) high-pressure natural gas stream is provided；
C) the high-pressure natural gas stream is divided into Part I and Part II；
D) Part I of cooling and the high-pressure natural gas stream that liquefies is to produce LNG stream；
E) the first refrigerating part is provided via the nitrogen kind of refrigeration cycle；
F) the second refrigerating part is provided by expanding the Part II of the high-pressure natural gas；And
G) using first refrigerating part and second refrigerating part come realize the high-pressure natural gas stream in step d) this The cooling and liquefaction of a part.
39. one kind is used for liquefaction of nitrogen device and the integration of natural gas liquefaction device to produce liquefied natural gas (" LNG ") and liquid nitrogen The method of (" LIN "), this method comprise the following steps：
A) the liquefaction of nitrogen device with the first nitrogen kind of refrigeration cycle is provided, the wherein liquefaction of nitrogen device includes turbine, booster and more A cooler, wherein the first nitrogen kind of refrigeration cycle are configured to provide refrigeration in first heat exchanger；
B) the second nitrogen kind of refrigeration cycle is provided, wherein the second nitrogen kind of refrigeration cycle includes the second turbine, the second booster and multiple the Two coolers, wherein the second nitrogen kind of refrigeration cycle are configured to provide refrigeration in second heat exchanger；
C) the first natural gas flow is purified in the first purification unit to remove first group of impurity, so that produce purifying first is natural Air-flow；
D) in the second heat exchanger using the refrigeration from the nitrogen kind of refrigeration cycle come first natural gas flow that cools down and liquefy To produce LNG stream, wherein first natural gas flow has LNG refrigeration demands, and wherein the LNG stream is in first pressure PHLower liquefaction；
E) the second natural gas flow is purified in the second purification unit to remove second group of impurity, so that produce purifying second is natural Air-flow；
F) second natural gas flow is partly cooled down in the second heat exchanger；
G) natural gas flow of part cooling is extracted from the centre portion of the second heat exchanger；
H) natural gas flow that the part cools down is made to press P in being expanded into natural gas expansion turbineMTo form cold natural gas flow, its In press P in thisMIn less than first pressure PHPressure；And
I) the cold natural gas flow is heated with this by carrying out heat exchange with first natural gas flow in the second heat exchanger The hot junction of second heat exchanger produces the natural gas flow of heating,
Wherein the natural gas expansion turbine drives the first booster,
Wherein the LNG refrigeration demands are provided by the combination from the second nitrogen kind of refrigeration cycle and the refrigeration of step i),
A part for the liquid nitrogen in the first nitrogen kind of refrigeration cycle is wherein extracted as product liquid nitrogen, wherein will at least equal portion The gaseous nitrogen divided shines to extract as product liquid nitrogen to be incorporated into the first nitrogen kind of refrigeration cycle as former state, and
Wherein the first nitrogen kind of refrigeration cycle and the second nitrogen kind of refrigeration cycle shares a common nitrogen recycle compressor.
40. method as claimed in claim 39, wherein first booster be configured to compress second natural gas flow or From the stream of second natural gas flow.
41. method as claimed in claim 39, wherein first booster are configured to compress stream selected from the group below, the group by The following forms：First natural gas flow, the first natural gas flow of the purifying, second natural gas flow, the second of the purifying Natural gas flow, the part cooling natural gas flow, the heating natural gas flow and the nitrogen kind of refrigeration cycle in nitrogen fluid.
42. method as claimed in claim 39, wherein first group of impurity is in first pressure PHIt is lower to have at or greater than first The solidification point of the condensing temperature of alkane.
43. method as claimed in claim 39, wherein second group of impurity include water.
44. method as claimed in claim 39, wherein the first nitrogen kind of refrigeration cycle further include nitrogen feed compressor.
45. method as claimed in claim 39, wherein the first nitrogen kind of refrigeration cycle are the kind of refrigeration cycle of closing.
46. method as claimed in claim 39, wherein first natural gas flow and second natural gas flow come from same day Right source of the gas.
47. method as claimed in claim 46, the wherein gas source are the days with the pressure between 15 and 100 absolute pressures Right feed channel.
48. method as claimed in claim 39, wherein first natural gas flow come from the first gas source, and this second day Right air-flow comes from the second gas source, and wherein first gas source and second gas source is different sources.
49. method as claimed in claim 48, wherein first gas source include natural gas line.
50. method as claimed in claim 49, the wherein natural gas line have the pressure between 15 and 100 absolute pressures.
51. method as claimed in claim 39, wherein first purification unit and second purification unit are same units.
52. method as claimed in claim 39, wherein first purification unit and second purification unit are separated units, Wherein first purification unit is configured at least remove water and carbon dioxide, and wherein second purification unit is configured to At least remove water.
53. method as claimed in claim 39, wherein the liquefaction of nitrogen device further include subcooler.
54. a kind of be used for the first liquefier and the second liquefier integration to produce the side of the first liquefied gas and the second liquefied gas Method, this method comprise the following steps：
A) the first liquefier with the first kind of refrigeration cycle is provided, wherein first liquefier includes recycle compressor, first Heat exchanger and turbocharger；
B) second kind of refrigeration cycle is provided, wherein second kind of refrigeration cycle is configured to provide refrigeration in second heat exchanger,
C) in the second heat exchanger by with second kind of refrigeration cycle carry out heat exchange come cool down and liquefy the first air-flow with Liquefied first air-flow is produced, wherein liquefied first air-flow is in first pressure；
D) the second flow expansion is made to second pressure to produce the second air-flow of expansion；And
E) the second air-flow of the expansion is heated in the second heat exchanger to produce the air-flow of heating,
Wherein a part for the first refrigerant gas in first kind of refrigeration cycle is extracted and liquefied and produces the first refrigerant gas Product liquid, wherein using the first refrigerant gas of gaseous state of at least moiety according to as the first refrigerant gas product liquid pumping Take out and be incorporated into as former state in first kind of refrigeration cycle,
Wherein in addition to the refrigeration provided by second kind of refrigeration cycle, step e) is provided for first gas that cools down and liquefy The refrigeration of stream, and
Wherein first kind of refrigeration cycle and second kind of refrigeration cycle shares a common recycle compressor.
55. method as claimed in claim 54, wherein first kind of refrigeration cycle are selected from by nitrogen kind of refrigeration cycle and hydrogen kind of refrigeration cycle The group of composition.
56. method as claimed in claim 54, wherein in step c) liquefied first air-flow from the expansion the Two air-flows, the wherein first pressure are roughly the same with the second pressure.
57. method as claimed in claim 54, wherein second kind of refrigeration cycle are selected from by nitrogen kind of refrigeration cycle and hydrogen kind of refrigeration cycle The group of composition.
58. method as claimed in claim 54, wherein cooling and liquefied first air-flow include natural gas in step c).
59. method as claimed in claim 54, wherein second air-flow of expansion includes natural gas in step d).
60. method as claimed in claim 54, the product liquid of wherein first refrigerant gas is liquid nitrogen.
61. a kind of be used for the first liquefier and the second liquefier integration to produce the side of the first liquefied gas and the second liquefied gas Method, this method comprise the following steps：
A) provide with using the first refrigerant the first kind of refrigeration cycle the first liquefier, wherein first kind of refrigeration cycle by with It is set in first heat exchanger and refrigeration is provided；
B) provide with using second refrigerant the second kind of refrigeration cycle the second liquefier, wherein second kind of refrigeration cycle by with It is set in second heat exchanger and refrigeration is provided；
C) cooled down in the first heat exchanger by carrying out heat exchange the first air-flow of cooling with first kind of refrigeration cycle with producing The first air-flow；
D) cooled down in the second heat exchanger by carrying out heat exchange the second air-flow of cooling with second kind of refrigeration cycle with producing The second air-flow；
E) the 3rd flow expansion is made to produce the 3rd air-flow of expansion；And
F) heated in the heat exchanger in the group being made of the first heat exchanger, the second heat exchanger and combinations thereof 3rd air-flow of the expansion to produce the air-flow of heating,
Wherein in addition to the refrigeration provided by second kind of refrigeration cycle, step f) provides the system for cooling down second air-flow It is cold,
Wherein in addition to the refrigeration provided by first kind of refrigeration cycle, step f) provides the system for cooling down first air-flow It is cold, and
Wherein first kind of refrigeration cycle and second kind of refrigeration cycle shares a common recycle compressor.
62. method as claimed in claim 61, wherein first and second kind of refrigeration cycle are nitrogen kind of refrigeration cycle.
63. method as claimed in claim 61, wherein first refrigerant and the second refrigerant have identical composition.
64. method as claimed in claim 61, wherein first air-flow are selected from the group, which is made of the following：Naturally Gas, ethane, ethene, acetylene, other C3-C6Alkane, alkene and alkynes and nitrogen, and wherein first air-flow is walked in cooling Rapid c) period liquefaction.
65. method as claimed in claim 61, wherein first air-flow are selected from the group that is made of hydrogen and helium, wherein this One air-flow does not liquefy during cooling step c).
66. method as claimed in claim 61, wherein the 3rd air-flow of expansion includes natural gas in step e).
67. method as claimed in claim 61 a, wherein part for first refrigerant in first kind of refrigeration cycle is taken out Take out and liquefy and produce liquid the first refrigerant product, wherein shining the first refrigerant of gaseous state of at least moiety as liquid First refrigerant extracts to be incorporated into first kind of refrigeration cycle as former state.
68. method as claimed in claim 61 a, wherein part for the second refrigerant in second kind of refrigeration cycle is taken out Take out and liquefy and produce liquid second refrigerant, made wherein shining the second refrigerant of at least moiety as liquid second Cryogen extracts to be incorporated into second kind of refrigeration cycle as former state.
69. one kind is used for liquefaction of nitrogen device and natural gas depressurization integration to produce the method for liquid nitrogen (" LIN "), this method includes Following steps：
A) the liquefaction of nitrogen device with nitrogen kind of refrigeration cycle is provided, the wherein liquefaction of nitrogen device includes nitrogen recycle compressor, heat Exchanger and the first turbocharger；
B) nitrogen stream is introduced under the conditions of effective for liquefaction nitrogen in the liquefaction of nitrogen device to produce liquid nitrogen product；
C) from first pressure PHThe source of lower operation extracts natural gas flow；
D) natural gas flow is purified in purification unit to produce the natural gas of purifying；
E) natural gas of the purifying is partly cooled down in the heat exchanger；
F) natural gas of part cooling is extracted from the centre portion of the heat exchanger；
G) natural gas that the part cools down is made to press P in being expanded into natural gas expansion turbineMTo form cold natural gas flow, wherein P is pressed in thisMIn less than first pressure PHPressure；And
H) in the heat exchanger by with from the nitrogen kind of refrigeration cycle nitrogen carry out heat exchange heat the cold natural gas flow with The natural gas flow of heating is produced from the hot junction of the heat exchanger,
Wherein step h) provides additional refrigeration to the liquefaction of nitrogen device so that with without step c)-i) method compared with, can To produce additional liquid nitrogen,
Wherein natural gas expansion turbine driving first gas booster.
70. the method as described in claim 69, wherein the first gas booster be configured to compress the natural gas flow or From its stream.
, should 71. the method as described in claim 69, wherein the first gas booster are configured to compress stream selected from the group below Group is made of the following：The natural gas flow, the natural gas flow of the purifying, natural gas flow, the day of the heating of part cooling Nitrogen fluid in right air-flow and the nitrogen kind of refrigeration cycle.
72. the method as described in claim 69, the wherein purification unit are configured at least remove water from the natural gas flow.
73. the method as described in claim 69, wherein the nitrogen kind of refrigeration cycle further include nitrogen feed compressor.
74. the method as described in claim 69, wherein the liquefaction of nitrogen device further include subcooler.
75. the method as described in claim 69, the wherein gas source include natural gas line.
76. the method as described in claim 75, the wherein natural gas line have the pressure between 15 and 100 absolute pressures.
77. one kind is used for liquefaction of nitrogen device and natural gas depressurization integration to produce the method for liquid nitrogen (" LIN "), this method includes Following steps：
A) the liquefaction of nitrogen device with nitrogen kind of refrigeration cycle is provided, the wherein liquefaction of nitrogen device includes nitrogen recycle compressor, heat Exchanger and at least one turbocharger；
B) nitrogen stream is introduced under the conditions of effective for liquefaction nitrogen in the liquefaction of nitrogen device to produce liquid nitrogen product；
C) natural gas flow is recycled from high-voltage power supply, the wherein natural gas flow is in first pressure；
D) natural gas flow is expanded into second pressure to produce the natural gas flow of expansion, wherein the second pressure be less than this The pressure of one pressure；And
E) natural gas flow of the expansion is heated in the heat exchanger to produce the natural gas flow of heating,
Wherein step e) provides additional refrigeration to the liquefaction of nitrogen device so that compared with without step d) to method e), Additional liquid nitrogen can be produced.
CN201680054318.5A 2015-08-06 2016-08-05 Method for producing liquefied natural gas Pending CN108027199A (en)

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US201662370953P 2016-08-04 2016-08-04
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