CN106164612A - The Claude process for manufacturing liquid gas improved - Google Patents
The Claude process for manufacturing liquid gas improved Download PDFInfo
- Publication number
- CN106164612A CN106164612A CN201580006400.6A CN201580006400A CN106164612A CN 106164612 A CN106164612 A CN 106164612A CN 201580006400 A CN201580006400 A CN 201580006400A CN 106164612 A CN106164612 A CN 106164612A
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- Prior art keywords
- gas
- mixed flow
- compressor
- decompressor
- stream
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- 239000007788 liquid Substances 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims description 10
- 238000001816 cooling Methods 0.000 claims abstract description 15
- 239000000203 mixture Substances 0.000 claims abstract description 15
- 238000010438 heat treatment Methods 0.000 claims abstract description 7
- 238000011084 recovery Methods 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 13
- 239000007789 gas Substances 0.000 description 64
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 36
- 239000003949 liquefied natural gas Substances 0.000 description 28
- 239000003345 natural gas Substances 0.000 description 13
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 239000002283 diesel fuel Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 235000009508 confectionery Nutrition 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- 239000005977 Ethylene Substances 0.000 description 2
- 230000003213 activating effect Effects 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 230000001050 lubricating effect Effects 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000003570 air Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012208 gear oil Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 235000012907 honey Nutrition 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
- F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—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"
- F25J1/0042—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 liquid expansion with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0284—Electrical motor as the prime mechanical driver
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant 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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A kind of system and method for liquid gas is provided.Described method includes that making input gas and first reclaim stream combines to form the first mixed flow, and by making the first mixed flow and the second mixed flow produce the first mixed flow of cooling and the second mixed flow of heating through heat exchanger.The method also includes gas and the mixture of liquid gas using the first decompressor to produce self cooled first mixed flow, and produces described liquid gas in exit.
Description
Technical field
The present invention is directed generally to energy technologies, and be more particularly directed to a kind of improvement for manufacturing liquid gas
Claude process.
Background technology
Gas is carried out liquefaction and would generally produce some requirements.Gaseous material, such as natural gas, as liquefied natural gas
(" LNG ") can relatively easily or more economic transport.Air, nitrogen, oxygen, hydrogen, helium and other liquid of liquefaction
Activating QI body is widely used in industry.
Manufacture liquid gas and at least need following steps: remove sensible heat and remove latent heat.
Have been developed over multiple technologies to manufacture liquid gas.Typical method uses the single component refrigerator of cascade,
Described single component refrigerator generally uses propane, ethylene and methane as working fluid.Recently, hybrid refrigeration is had been developed for
Agent system, this mixed refrigerant systems uses nitrogen, methane, ethylene, propane and the mixture of butane.Oldest being used for manufactures liquid
One of method of activating QI body is based on Claude process, and it uses the combination of compressor and decompressor to make gas turn cold.Final
In step, the gas turned cold of high pressure passes Joule-Thomson choke valve, and a part for gas liquefies in this choke valve.Fig. 1
In show a kind of example system using Claude process.Pretreated natural gas through heat exchanger to reduce its temperature,
Then the natural gas cooled down is transformed into liquefied natural gas through Joule-Thomson valve with the natural gas some cooled down.Fig. 1 is
Other elements of system run the temperature of the temperature so that working fluid to be cool below pretreated natural gas, and make cooling
Working fluid passes heat exchanger, so that heat is delivered to working fluid with cooled natural gas from natural gas.Although Fig. 1's is
System is shown as making natural gas liquefaction, but it is to be understood that, this system may be used for other gases that liquefy.Additionally, should manage
Solving, the working fluid being compressed and expanded can be identical with pretreated unstripped gas, or can be different.
Summary of the invention
According to the first embodiment of the present invention, the system for liquid gas includes the first colligator, the first colligator by
The combination of input gas and the first Part I reclaiming stream forms the first mixed flow.This system also includes that heat exchanger, heat are handed over
Heat is delivered to the second mixed flow from described first mixed flow by parallel operation, produces the first mixed flow of cooling and the second of heating mixes
Interflow.This system also includes: the first decompressor, and the first decompressor is produced gas and liquid gas by the first mixed flow cooled down
Mixture；And outlet, it is used for producing liquid gas.This system still further comprises the first compressor, the first compressor origin
The second recovery stream is produced from the gas of gas and the described mixture of liquid gas.This system also includes the second colligator, second
Colligator is reclaimed stream by described second and the 3rd recovery stream forms described second mixed flow and provided extremely by described second mixed flow
Described heat exchanger.This system also includes the second compressor, and the of the heating from described heat exchanger received by the second compressor
Two mixed flows also produce described first recovery stream, and the Part I reclaiming stream by described first provides the most described first to combine
Device.This system still further comprises the second decompressor, and the second decompressor is received described first to reclaim the Part II of stream, manufactured institute
State the 3rd recovery stream and reclaim stream offer by the described 3rd to described second colligator.
According to the second embodiment of the present invention, a kind of method of liquid gas, the method includes: make input gas and first
The Part I reclaiming stream combines, to form the first mixed flow.The method also includes: by making the first mixed flow and the second mixing
Flowing through the second mixed flow of the over-heat-exchanger the first mixed flow and heating to produce cooling, described heat exchanger is suitable to heat
It is delivered to described second mixed flow from described first mixed flow.Described method also includes: use the first decompressor to produce from institute
State gas and the mixture of liquid gas of the first mixed flow of cooling；And liquid gas is produced in exit.The method is also
Farther include: use the first compressor to be produced the second recovery by the gas of the described mixture from gas and liquid gas
Stream；And make described second recovery stream and the 3rd reclaim stream combination, to form described second mixed flow.The method also includes: make
The described first Part I reclaiming stream and Part II is produced by the second mixed flow heated with the second compressor；And use
Second decompressor is produced the described 3rd by the described first Part II reclaiming stream and reclaims stream.
According to the third embodiment of the invention, a kind of gas liquefaction system, swollen including heat exchanger and gerotor formula
Swollen machine.Described heat exchanger is received input gas and produces the gas of cooling.Described gerotor formula decompressor is received described
The gas cooled down the mixture producing gas and liquid gas.
Before proceeding by detailed description below, set for specific vocabulary and the phrase used in the whole text in this patent document
Put definition and be probably favourable: term " includes (include) " and " including (comprise) " and its derivative represent and be not subject to
Limit comprises；Term "or" is inclusive, represent and/or；Phrase " with ... be associated " and " associated with it " and its
Derivative can represent include, be included in inside, interconnect, comprise, be included in inside, be connected to or with ... be connected, join
Receive or with ... be connected and ... connection and ... coordinate, interlock, arranged side by side, close, be bonded to or with ... bond, have, have
Have ... character or similar meaning.
Accompanying drawing explanation
In order to be more fully understood from the present invention and advantage thereof, referring now to being described below that the appended accompanying drawing of combination is given, its
In, identical reference represents identical parts:
Fig. 1 illustrates the example system using Claude process to carry out liquefied natural gas；
Fig. 2 illustrates the first system for liquid gas according to the present invention；
Fig. 3 illustrates the second system for liquid gas according to the present invention；
Fig. 4 illustrates the gas of the appropriate function as the gas temperature in the system of liquefied methane according to the present invention
Body pressure；
Fig. 5 illustrates the energy expenditure of the system for liquefied methane according to the present invention；
Fig. 6 illustrates the calculating process assuming to manufacture the theoretical minimal energy consumption of LNG when gas is pure methane；
Fig. 7 illustrates the usual energy expenditure of the distinct methods manufacturing LNG.
Detailed description of the invention
I.e. should be appreciated that starting, although be hereafter illustrated example embodiment, but the present invention can use any amount
Technology implement, the most currently known or unknown.The present invention should never be by the example gone out illustrated in following
Property implement, accompanying drawing and the restriction of technology.It addition, accompanying drawing has not necessarily been drawn to scale.
Fig. 2 shows the system 200 for liquefied natural gas according to the present invention.This system 200 is similar to Claude process,
But decompressor 202 instead of Joule-Thomson valve.In fig. 1 and 2, liquefaction process is incomplete, and therefore LNG discharges
Mouth comprises the gas that must be recovered.Decompressor 202 allow larger portion of gas liquefaction and thus improve system 200 relative to
The efficiency of the system shown in Fig. 1.But, decompressor 202 allows for bearing the existence of liquid.
Power decompressor (such as, centrifugal, axial type) must run with high end speed, and this makes equipment be vulnerable to liquid
The impact corroded.On the contrary, positive-displacement expansion engine (such as, reciprocating, spiral, slide sheet type and gerotor formula) is at relatively low speed
Degree is lower to be run and can more easily bear liquid.But, reciprocating expansion engine has the valve can interfered with liquid outlet,
This makes to risk the risk damaging machine when reciprocating-piston attempts the liquid of compression reservation.Spiral and sliding vane type expander is all
Needing for lubrication and the lubricating fluid of sealing purpose, the liquid gas that lubricating fluid produces with decompressor mixes and must be
Additional step subsequently is removed.Because decompressor is the coldest, therefore, it is difficult to find the conjunction keeping liquid at cryogenic temperatures
Suitable lubricant.On the contrary, gerotor does not have these operation shortcomings.Generally, other decompressor has according to yardstick
There is the efficiency of about 50% to 80%.On the contrary, gerotor formula decompressor has the efficiency of 80% to 90%, this it is required that
Gas liquefaction system according to the present invention is attractive in economy.
The StarRotor company of Tennessee State institute station (College Station) has been developed for one and may be used for
According to the gerotor formula decompressor in the gas liquefaction system of the present invention.Only certain embodiments of the present invention can utilize in example
As public in U.S. Patent No. 7186101, U.S. Patent No. 7695260 and U.S. Patent Publication the 2011/0200476th
The technology of other StarRotor opened, the full content of these three patent is incorporated herein by.
Being prepared by optimization method, the Claude process of improvement has been particularly efficient and close to manufacturing the theory of LNG
Little energy requirement.By inferring, the method should have similar efficiency for other gases.The further advantage of the method
Be its simplicity and its need not the extra work fluid beyond the gas that is liquefied.
Fig. 3 illustrates the system 300 for liquid gas according to the present invention.This system 300 exemplifies liquefied natural gas
Method, but this system 300 can be designed to any gas that liquefies.In figure 3, line pressure (about 5.3MPa or
780psia) and supply the natural gas flow 302 of input at a temperature of about 35 DEG C (or 95 °F).If gas under high pressure can not be obtained
Body, then need extra compression step with under high pressure supply gas.
Line gas 302 mixes with the first recovery stream 306 from compressor section 308 at colligator 304.First mixes
Sensible heat exchanger 310 is flow through at interflow 309, and the first mixed flow is pre-cooled to temperature T in sensible heat exchanger2.Then, first
Mixed flow 309 flows through decompressor E1, and in decompressor E1, pressure is lowered to about 0.1MPa (1 atmospheric pressure).It is operated in expansion
Being brought out in machine E1, this makes axle 312 rotate.
Decompressor E1 cools down the first mixed flow 309 and makes the part liquefaction of the first mixed flow.Produce LNG 315 from
Decompressor outlet in container 316 eliminates and manufactures at outlet 314.The natural gas remaining steam 318 is recovered
And it being supplied to compressor C1, it is compressed into pressure P and temperature T at compressor C11, to form the second recovery stream 322.As hereafter
In will be described in more detail, compressor C1 is by axle 312 energy supply.
Second reclaims stream 322 mixes with the 3rd recovery stream 326 from compressor section 308, with shape at colligator 324
Becoming the second mixed flow 328, the second mixed flow passes sensible heat exchanger 310.The temperature of the second mixed flow 328 is than the first mixed flow
309 is cold, and therefore the second mixed flow 328 extracts heat from the first mixed flow 309 and warms.Second mixed flow 328 is with about 25 DEG C
Reveal and be transported to compressor section 308 from sensible heat exchanger 310.
The heat exchanger of Fig. 1 and Fig. 2 includes the working fluid of the compression from booster compressor, and booster compressor is along warm
A part for exchanger rather than whole length.As a result, the thermic load in the different sections of heat exchanger is different, and this makes can not
Substantially homogeneous temperature difference can be maintained along length.In the some parts of heat exchanger, temperature difference can be bigger, and this causes fall
The thermodynamics irreversibility of low-yield efficiency.
On the contrary, the heat exchanger 310 of system 300 only includes the first mixed flow 309 and the second mixed flow 328, the first mixing
Stream and the second mixed flow flow along whole length.Further, the mass flow of two described streams is substantially the same.This permits
Permitted heat exchanger 310 and between the first mixed flow 309 and the second mixed flow 328, maintained essentially constant temperature along its length
Difference.This uniform and little temperature difference reduces thermodynamics irreversibility, thus improves energy efficiency.
In compressor section 308, the second mixed flow 328 is compressed in a series of compressors carry out interstage cooling.
As described in greater detail below, the compressor of compressor section 308 is by axle 312 energy supply.In fig. 3 it is shown that five compressions
Level；However, it is possible to use more or less of level.More level will improve efficiency, this is because compression is close to isothermy.
Less level will reduce capital cost.
The compressed gas 330 leaving compressor section 308 is divided into two parts.Part I, i.e. first reclaims stream 306,
Mix, as mentioned above with the line gas 302 entered.In some constructions, line gas 302 have substantially with compressed gas
The temperature and pressure that 330 (and first recovery streams 306) are identical.But, in other construct, temperature and/or pressure may not
With.The Part II of compressed gas 330, i.e. flows 332, is coupled to decompressor E2.Being operated in decompressor E2 and be brought out, this makes
Axle 312 rotates.The ejection of decompressor E2, the i.e. the 3rd reclaims stream 326, at colligator 324 with from the second of compressor C1
Reclaim stream 322 mixing.
As it has been described above, single drive shaft 312 can be common to all decompressors and the compressor of system 300.From decompressor
The work that E1 and E2 draws contributes to making axle 312 rotate.Then, axle 312 runs so that compressor C1 to C6 rotates.Motor 334
It is also connected to axle 312, to compensate the poor efficiency in the parts of system 300, and provides during liquefaction line gas 302 by being
The work that system 300 completes.
Following equations further describes the design of system 300,
Q=(1+m) (Hh,o-Hh,i)=-n (Hl,o-Hl,i)
Wherein, Q=is the thermic load of heat exchanger 310, and m=reclaims the quality of the compressed gas in stream 306, n=second
The quality of the gas in mixed flow 328, Hh,iThe enthalpy of the first mixed flow 309 of=entrance heat exchanger 310, Hh,o=leave heat friendship
The enthalpy of the first mixed flow 309 of parallel operation 310, Hl,iThe enthalpy of the second mixed flow 328 of=entrance heat exchanger 310, and Hl,o=
Leave the enthalpy of the second mixed flow 328 of heat exchanger 310.Further,
In order to improve efficiency, the pressure of the compressed gas 330 leaving compressor section 308 is chosen to its entropy with flat
Weigh substantially the same in the entropy of the steam 318 of LNG 315.By following these rules and assuming to carry out isentropic Compression/expansion, from
Compressor C1 with decompressor E2 expellant gas temperature by identical, this eliminate in colligator 324 with mix different temperatures two
Plant the poor efficiency that gas is relevant.Fig. 4 show as the function from compressor section 308 expellant gas temperature from compressor section
The appropriate Theoretical gas pressure that section 308 is discharged.
It is emphasized that the pressure and temperature of middle use exemplified above is only example.LNG 315 can be stored in
Under pressure beyond 0.1MPa, line gas 302 can beyond pressure beyond 5.3MPa and 35 DEG C at a temperature of supply.For
Acquisition optimal performance, it may be necessary to make the line gas 302 compress in advance or expand in advance, to leave pressure in matching system 300
The pressure of compressor portion section 308.
Fig. 5 shows as heat exchanger entrance temperature T1And the letter of the efficiency of all compressors and decompressor in system
The energy expenditure of the system 300 of number, for simplicity, it is assumed that all of compressor and decompressor are identical.Energy expenditure is " sweet
Honey point (sweet spot) " (T1=-90 to-95 DEG C；P=0.7MPa) place is minimum.At sweet spot, correspondingly compressor/
When efficiency of expander is 95%-80%, energy expenditure is 0.18-0.30kWh/kg.It should be noted that, the energy of report in Fig. 5
Consumption is Utopian and does not include compressor and the impact to mass flow of the decompressor poor efficiency.
Fig. 6 calculates the theoretical minimal energy consumption (0.147kWh/kg) of the system of any manufacture LNG.This value is similar to
In literature value (0.133kWh/kg), document value employs slightly different reference conditions.See C.W.Remeljej and
" radiation instinct analysis (the An exergy of little yardstick liquefied natural gas (LNG) liquifying method of A.F.A.Hoadley
Analysis of small-scale liquefied natural gas (LNG) liquefaction processes) ",
" energy " 2005-2019 (2006) phase page 31 (" Remeljej ").
Assume that compressor and decompressor have the efficiency of about 90%, then energy expenditure is 0.22kWh/kg LNG.Assume electricity
Price is 0.036 dollar/kWh, and this is equivalent to the bavin of diesel oil equivalent-substantially two cent per gallon of 0.0203 dollar/gallon
Oil equivalent.In the world, LNG factory produces about 5,000,000 tons every year.See Remeljej " at 0.036 dollar/kWh
Under price, energy expenditure is reduced to 0.22kWh/kg from 0.35kWh/kg and saves 23,400,000 dollars of (Reducing every year
energy consumption from0.35to0.22kWh/kg saves$23.4million per year at$0.036/
kWh)”。
The energy efficiency (compressor efficiency of 90%) highlighted under large scale discussed above.Even if it is under little yardstick, interior
Gear oil pump type compressor is also very efficient (efficiency of about 85%)；Therefore, system 300 will allow to service goods fortune
Multiple region LNG factories of defeated route reduce in proportion, and need not transport substantial amounts of LNG on a highway.Discussed above right
It is also suitable in a region factory.
Region LNG factory will include that efficiency is of about compressor and the decompressor of 85%.Under this level of efficiency, energy disappears
Consumption is 0.26kWh/kg LNG.This energy expenditure can be described as the percentage ratio of the interior energy of natural gas,
If engine is the efficiency of 40%, then the natural gas of 4.2% must burn to liquefy remaining 95.8%.
Based on when describing with volume in conventional elements, energy expenditure is the LNG of 0.417kWh/gal.
Zero potential energy is of about 0.12 dollar/kWh [5]；Therefore, one gallon of natural gas of liquefaction spends 0.05 dollar--about
Per gallon LNG spends 5 cents.Describing per gallon diesel oil equivalent, the cost of energy of liquefaction LNG is:
Again, it is assumed that electricity price is 0.12 dollar/kWh, and this is equivalent to the diesel oil equivalent of 0.08 dollar/gal--
It it is ten cents every about gallons of diesel fuel equivalent.
As shown in Figure 7, little simple LNG system needs the energy of 2 to 3 times of system 300.Based on diesel oil equivalent
Time, the cost of energy of these systems about per gallon diesel oil equivalent is 0.16 to 0.24 dollar.
System described herein, equipment and method can be modified, increase or deleted, without deviating from the present invention's
Scope.The parts of system and equipment can be integrated or separate.Additionally, the operation of system and equipment can by more,
Less or other parts perform.Method can include more, fewer, or other step.Furthermore it is possible to any suitable
Order performs these steps.As used in this application, each component during " each " represents a group or the subgroup of a group
In each component.
In order to help the right appended by any reader understanding of auditor and any patent based on the application mandate to want
Asking, it is intended that remind at this, any appended claim or claim feature are because in the applying date of the application being
There is the content without regard to United States patent law 35U.S.C Section 112 the 6th section, except clearly making in requiring in specific rights
With term " be used for ... device " or " be used for ... step ".
Claims (20)
1. a gas liquefaction system, including:
First colligator, is suitable to be formed the first mixed flow by the combination of input gas and the first Part I reclaiming stream；
Heat exchanger, is suitable to receive described first mixed flow and the second mixed flow, is delivered to from described first mixed flow by heat
Described second mixed flow, produces the first mixed flow and second mixed flow of heating of cooling；
First decompressor, is suitable to receive the first mixed flow of described cooling and produce the mixture of gas and liquid gas；
Outlet, is suitable to produce described liquid gas；
First compressor, is suitable to receive from gas and the gas of the described mixture of liquid gas and produce the second recovery stream；
Second colligator, is suitable to be reclaimed stream by described second and the 3rd recovery stream forms described second mixed flow and by described second
Mixed flow provides to described heat exchanger；
Second compressor, is suitable to receive the second mixed flow of the heating from described heat exchanger and produce described first reclaim
Stream, and be suitable to reclaim the Part I offer of stream by described first to described first colligator；
Second decompressor, is suitable to receive the described first Part II reclaiming stream, manufactures the described 3rd and reclaim stream and by described the
Three reclaim stream provides to described second colligator.
Gas liquefaction system the most according to claim 1, wherein, one or more in described decompressor and compressor are
Gerotor.
Gas liquefaction system the most according to claim 1, wherein, described second compressor includes carrying out the one of interstage cooling
Series of compressor.
Gas liquefaction system the most according to claim 1, wherein, described heat exchanger fits along its whole length in institute
State and between the first mixed flow and described second mixed flow, maintain essentially constant temperature poor.
Gas liquefaction system the most according to claim 1, wherein, described second compressor is suitable to produce the first recovery stream,
Described first entropy reclaiming stream substantially mixes with the gas carrying out the most described first decompressor generation and the described of liquid gas
The entropy of the gas of thing is identical.
Gas liquefaction system the most according to claim 1, wherein, the temperature and pressure of described input gas with leave described
The temperature and pressure of the gas of the second compressor substantially mates.
Gas liquefaction system the most according to claim 1, wherein, described first decompressor, described first compressor, described
Second compressor and described second decompressor are connected to the axle shared.
Gas liquefaction system the most according to claim 7, farther includes motor, and described motor is connected to described shared
Axle, is adapted to provide for power to the poor efficiency in the parts compensating described gas liquefaction system, and provides in the mistake manufacturing liquid gas
The work completed by described gas liquefaction system in journey.
Gas liquefaction system the most according to claim 2, wherein, in described decompressor and compressor one or more
Run in the range of 80% to 90% efficiency.
10. a method for liquid gas, the method includes:
The Part I making input gas and first reclaim stream combines, to form the first mixed flow；
By making the first mixed flow and the second mixed flow produce the of the first mixed flow of cooling and heating through heat exchanger
Two mixed flows, described heat exchanger is suitable to from described first mixed flow, heat is delivered to described second mixed flow；
The first decompressor is used to produce gas and the mixture of liquid gas of the first mixed flow from described cooling；
Liquid gas is produced in exit；
The first compressor is used to be produced the second recovery stream by the gas of the described mixture from gas and liquid gas；
Make described second to reclaim stream and the 3rd recovery stream combines, to form described second mixed flow；
The second compressor is used to be produced the described first Part I reclaiming stream and Part II by the second mixed flow heated；
Use the second decompressor to be produced the described 3rd by the described first Part II reclaiming stream and reclaim stream.
11. methods according to claim 10, wherein, one or more in described decompressor and compressor are internal gears
Oil pump.
12. methods according to claim 10, wherein, described second compressor includes a series of pressures carrying out interstage cooling
Contracting machine.
13. methods according to claim 10, farther include the whole length along described heat exchanger described
Maintain essentially constant temperature poor between one mixed flow and described second mixed flow.
14. methods according to claim 10, farther include to produce described first and reclaim stream so that this first recovery stream
Entropy substantially with the entropy phase of the gas of the described mixture coming gas that freely the most described first decompressor produces and liquid gas
With.
15. methods according to claim 10, wherein, the temperature and pressure of described input gas is pressed with leaving described second
The temperature and pressure of the gas of contracting machine substantially mates.
16. methods according to claim 10, wherein, described first decompressor, described first compressor, described second pressure
Contracting machine and described second decompressor are connected to the axle shared.
17. methods according to claim 16, farther include to use motor to provide power to described shared axle, its
In, the poor efficiency in the parts of the method that this power compensation performs described liquid gas, and provide at the described liquid gas of execution
The work completed during method.
18. methods according to claim 11, wherein, in described decompressor and compressor one or more 80% to
Run in the range of 90% efficiency.
19. 1 kinds of gas liquefaction systems, including:
Heat exchanger, is suitable to receive input gas and produce the gas of cooling；With
Gerotor formula decompressor, is suitable to receive the gas of described cooling and produce the mixture of gas and liquid gas.
20. gas liquefaction systems according to claim 19, wherein, described heat exchanger is further adapted for receiving working fluid also
From described input gas, heat is delivered to described working fluid, and described gas liquefaction system farther includes:
Be suitable to be cool below by described working fluid described input gas before described working fluid enters described heat exchanger
The system of the temperature of the temperature of body.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201461932596P | 2014-01-28 | 2014-01-28 | |
| US61/932,596 | 2014-01-28 | ||
| PCT/US2015/013349 WO2015116719A1 (en) | 2014-01-28 | 2015-01-28 | Modified claude process for producing liquefied gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106164612A true CN106164612A (en) | 2016-11-23 |
Family
ID=53678701
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|---|---|---|---|
| CN201580006400.6A Pending CN106164612A (en) | 2014-01-28 | 2015-01-28 | The Claude process for manufacturing liquid gas improved |
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| Country | Link |
|---|---|
| US (1) | US20150211788A1 (en) |
| CN (1) | CN106164612A (en) |
| AU (1) | AU2015211000A1 (en) |
| WO (1) | WO2015116719A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101792708B1 (en) * | 2016-06-22 | 2017-11-02 | 삼성중공업(주) | Apparatus of fluid cooling |
| CN106225420A (en) * | 2016-08-19 | 2016-12-14 | 浙江智海化工设备工程有限公司 | A kind of large-scale oxygen/nitrogen liquefaction plant of band deep freeze refrigerator |
| US10890181B2 (en) | 2019-06-13 | 2021-01-12 | Boundary Lubrication Systems, L.L.C. | Enhancing fluid flow in gerotor systems |
| WO2021254597A1 (en) * | 2020-06-16 | 2021-12-23 | Wärtsilä Finland Oy | A system for producing liquefied product gas and method of operating the same |
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|---|---|---|---|---|
| US3616652A (en) * | 1966-09-27 | 1971-11-02 | Conch Int Methane Ltd | Process and apparatus for liquefying natural gas containing nitrogen by using cooled expanded and flashed gas therefrom as a coolant therefor |
| US20030000213A1 (en) * | 1999-12-17 | 2003-01-02 | Christensen Richard N. | Heat engine |
| CN101223260A (en) * | 2005-07-19 | 2008-07-16 | 信永重工业株式会社 | Lng bog reliquefaction apparatus |
| CN102334001A (en) * | 2008-11-18 | 2012-01-25 | 气体产品与化学公司 | Liquefaction method and system |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB0120272D0 (en) * | 2001-08-21 | 2001-10-10 | Gasconsult Ltd | Improved process for liquefaction of natural gases |
| US6889522B2 (en) * | 2002-06-06 | 2005-05-10 | Abb Lummus Global, Randall Gas Technologies | LNG floating production, storage, and offloading scheme |
| EP1711685B1 (en) * | 2004-01-23 | 2015-09-16 | Starrotor Corporation | Gerotor apparatus for a quasi-isothermal brayton cycle engine |
| EP1929227B1 (en) * | 2005-08-09 | 2019-07-03 | Exxonmobil Upstream Research Company | Natural gas liquefaction process for lng |
| US8591199B2 (en) * | 2007-01-11 | 2013-11-26 | Conocophillips Company | Multi-stage compressor/driver system and method of operation |
| US8459048B2 (en) * | 2010-07-23 | 2013-06-11 | Nissan North America, Inc. | Gerotor expander for an air conditioning system |
| FR2977015B1 (en) * | 2011-06-24 | 2015-07-03 | Saipem Sa | METHOD FOR LIQUEFACTING NATURAL GAS WITH TRIPLE FIRM CIRCUIT OF REFRIGERATING GAS |
-
2015
- 2015-01-28 WO PCT/US2015/013349 patent/WO2015116719A1/en active Application Filing
- 2015-01-28 AU AU2015211000A patent/AU2015211000A1/en not_active Abandoned
- 2015-01-28 CN CN201580006400.6A patent/CN106164612A/en active Pending
- 2015-01-28 US US14/607,983 patent/US20150211788A1/en not_active Abandoned
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3616652A (en) * | 1966-09-27 | 1971-11-02 | Conch Int Methane Ltd | Process and apparatus for liquefying natural gas containing nitrogen by using cooled expanded and flashed gas therefrom as a coolant therefor |
| US20030000213A1 (en) * | 1999-12-17 | 2003-01-02 | Christensen Richard N. | Heat engine |
| CN101223260A (en) * | 2005-07-19 | 2008-07-16 | 信永重工业株式会社 | Lng bog reliquefaction apparatus |
| CN102334001A (en) * | 2008-11-18 | 2012-01-25 | 气体产品与化学公司 | Liquefaction method and system |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2015116719A1 (en) | 2015-08-06 |
| US20150211788A1 (en) | 2015-07-30 |
| AU2015211000A1 (en) | 2016-09-01 |
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