CN110186251A - It is a kind of to recycle natural gas liquefaction devices and method suitable for ultra-large three - Google Patents
It is a kind of to recycle natural gas liquefaction devices and method suitable for ultra-large three Download PDFInfo
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- CN110186251A CN110186251A CN201910500987.6A CN201910500987A CN110186251A CN 110186251 A CN110186251 A CN 110186251A CN 201910500987 A CN201910500987 A CN 201910500987A CN 110186251 A CN110186251 A CN 110186251A
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- Prior art keywords
- propane
- cmr
- wmr
- heat exchanger
- compressor
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 156
- 239000003345 natural gas Substances 0.000 title claims abstract description 68
- 238000000034 method Methods 0.000 title abstract description 37
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 400
- 239000001294 propane Substances 0.000 claims abstract description 200
- 238000001816 cooling Methods 0.000 claims abstract description 92
- 230000004087 circulation Effects 0.000 claims abstract description 22
- 230000001105 regulatory effect Effects 0.000 claims abstract description 12
- 238000004781 supercooling Methods 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 23
- 238000005057 refrigeration Methods 0.000 claims description 20
- 239000007791 liquid phase Substances 0.000 claims description 18
- 239000012071 phase Substances 0.000 claims description 17
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 10
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 239000000872 buffer Substances 0.000 claims description 2
- 239000000110 cooling liquid Substances 0.000 claims description 2
- 239000007792 gaseous phase Substances 0.000 claims description 2
- 238000003860 storage Methods 0.000 claims description 2
- 230000008092 positive effect Effects 0.000 abstract description 2
- 239000002994 raw material Substances 0.000 abstract description 2
- 238000010276 construction Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 238000004519 manufacturing process 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
- 230000000694 effects Effects 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 210000000582 semen Anatomy 0.000 description 1
- 239000000126 substance Substances 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"
- F25J1/0042—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
- F25J1/003—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
- F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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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
- F25J1/003—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
- F25J1/0047—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 an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
- F25J1/0057—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 an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream after expansion of the liquid refrigerant stream 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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/008—Hydrocarbons
- F25J1/0087—Propane; Propylene
-
- 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
- F25J1/0211—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0217—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle
- F25J1/0218—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 multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as at least a three level refrigeration cascade with at least one MCR cycle with one or more SCR cycles, e.g. with a C3 pre-cooling cycle
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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
- F25J1/02—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
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0262—Details of the cold heat exchange system
- F25J1/0263—Details of the cold heat exchange system using different types of heat exchangers
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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
- F25J1/02—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.
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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
- F25J1/02—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
Abstract
It includes natural gas liquefaction pipeline, the propane pre-cooling circulatory system, WMR cooling cycle system and CMR cooling cycle system that the invention discloses a kind of suitable for three ultra-large circulation natural gas liquefaction devices and method, device.Compared with prior art, the positive effect of the present invention is: the present invention is based on three circulations, share every grade of cooling load, natural gas passes sequentially through 1 plate-fin heat exchanger and 2 wound tube heat exchangers are cooled down, until liquefaction supercooling, process equipment quantity is few, and natural gas liquefaction device scale can reach single-row 600~8,000,000 tons/year；Cooling capacity needed for liquefaction process is provided by three propane, WMR azeotrope, CMR azeotrope systems, and system regulating measure is abundant, can provide matched cooling capacity for gas deliquescence process, flexible operation and good to adaptability to raw material.
Description
Technical field
It is specially a kind of natural suitable for three ultra-large circulations the present invention relates to natural gas liquefaction cryogenics field
Gas liquefaction device and method distributes the load of precooling zone, liquefaction stages and super cooled sect, using height by using three-level refrigeration cycle
Equipment is imitated, simple flow meets 600~8,000,000 tons/year of ultra-large natural gas liquefaction device construction demands of single-row production capacity.
Background technique
With the continuous development of LNG technical equipment, LNG factory construction general trend is developed towards enlargement in the world,
Single-row production capacity is mostly in 300~5,500,000 tons/year of scales, and maximum-norm is up to 7,800,000 tons/year.Extensive LNG dress in the world
Setting up the liquefaction process technology for setting use mainly has C3MR, DMR and AP-X technique of APCI company, Cophi Co., Ltd
Optimized Cascade technique, the MFC technique of Linde company and the DMR technique of Shell company.Large-scale LNG device
It can reduce unit LNG production cost, realize scale and benefit.
The domestic single-row maximum-norm of LNG device is 1,200,000 tons/year, using multistage one pack system refrigeration liquefying technique (MSC work
Skill).Realize the exploitation of single-row 3,500,000 tons/year of natural gas liquefaction process packets based on MSC technique, but the technique be unable to satisfy it is single-row
600~8,000,000 tons/year of ultra-large LNG plant constructions.
Therefore, a kind of natural gas liquid that can be suitably used for 600~8,000,000 tons/year of ultra-large natural gas liquefaction devices is developed
Chemical industry skill is very necessary.
Summary of the invention
The shortcomings that in order to overcome the prior art, the present invention provides a kind of suitable for three ultra-large circulation natural gas liquids
Change device and method, has the advantages that process is succinct, low energy consumption.
The technical scheme adopted by the invention is that: it is a kind of suitable for three ultra-large circulation natural gas liquefaction devices, packet
Include natural gas liquefaction pipeline, the propane pre-cooling circulatory system, WMR cooling cycle system and CMR cooling cycle system, in which:
The natural gas liquefaction pipeline is flashed by propane heat exchanger, WMR heat exchanger, CMR heat exchanger, LNG expanding machine, LNG
Tank and LNG booster pump are sequentially connected composition；
The propane pre-cooling circulatory system includes propane heat exchanger, propane compressor, propane compressor outlet cooler, height
Propane knockout drum, middle pressure propane gas-liquid liquid separation tank and low-pressure propane knockout drum are pressed, for natural gas, WMR cryogen
It is pre-chilled with CMR cryogen；
The WMR cooling cycle system includes WMR heat exchanger, the suction port of compressor WMR surge tank, WMR compressor, WMR pressure
Contracting machine exports cooler and WMR expanding machine, for the further cooling and partial liquefaction of natural gas, CMR cryogen；
The CMR cooling cycle system includes CMR heat exchanger, the suction port of compressor CMR surge tank, CMR compressor, CMR pressure
Contracting machine exports cooler and CMR expanding machine, for providing cooling capacity for natural gas and CMR cryogen whole liquefaction and supercooling.
The invention also discloses a kind of suitable for three ultra-large circulation natural gas liquefactions, includes the following steps:
1) propane cycles system is natural gas, WMR cryogen and the pre-cooling of CMR cryogen provide cooling capacity:
The propane being pressurized from propane compressor is divided into two strands after propane cooler is cooling, and wherein one liquid phase propane passes through
Enter propane heat exchanger after first high pressure propane throttle valve reducing pressure by regulating flow power, is mentioned for natural gas, WMR cryogen and the cooling of CMR cryogen
Semen donors, the phase propane come out from propane heat exchanger return to propane compressor high pressure suction inlet；Another strand of liquid phase propane passes through
Enter high pressure propane knockout drum after second high pressure propane throttle valve reducing pressure by regulating flow power and carry out gas-liquid separation, in which: head space gas
Phase propane returns to propane compressor high pressure suction inlet, and tank bottom liquid phase is divided into two strands, and wherein one liquid phase propane passes through presses in first
After propane throttle valve reducing pressure by regulating flow power enter propane heat exchanger, for natural gas, WMR cryogen and CMR cryogen continue cool down provide it is cold
Amount, the phase propane come out from propane heat exchanger, which returns to, presses suction inlet in propane compressor；Another strand of liquid phase propane passes through second
Propane knockout drum is pressed to carry out gas-liquid separation in entering after middle pressure propane throttle valve reducing pressure by regulating flow power, tank deck phase propane returns to
Suction inlet is pressed in propane compressor, the liquid phase propane of tank bottom exchanges heat by entering propane after low-pressure propane throttle valve reducing pressure by regulating flow power
Device continues cooling for natural gas, WMR cryogen and CMR cryogen and provides cooling capacity, and the phase propane come out from propane heat exchanger is through too low
Propane compressor low pressure suction port is returned to after pressure propane knockout drum；Low-pressure propane, middle pressure propane, high pressure propane are through propane pressure
It is recycled after the pressurization of contracting machine；
2) WMR refrigeration system is natural gas, further cooling and partial liquefaction provides cooling capacity to CMR cryogen:
The WMR cryogen come out from WMR exchanger base enters the suction port of compressor WMR surge tank, simultaneously through WMR compressor boost
After WMR cooler is cooling, into cooling liquid in propane heat exchanger；Liquid WMR enter WMR heat exchanger further cool down after from
Top comes out, and WMR heat exchanger is entered back into after WMR expander to low pressure, is natural gas, WMR cryogen and CMR cryogen into one
Step is cooling and partial liquefaction provides cooling capacity；It is slow that the low pressure WMR cryogen come out from WMR exchanger base returns to the suction port of compressor WMR
It is recycled after rushing tank；
3) CMR refrigeration system is natural gas and CMR cryogen all liquefies and supercooling provides cooling capacity:
CMR cryogen successively exchanges heat through CMR cooler, propane heat exchanger, WMR heat exchanger, CMR after CMR compressor boost
It is come out at the top of CMR heat exchanger after device is cooling, then enters back into CMR heat exchanger after CMR expander to low pressure, be natural gas
Supercooling provides cooling capacity with itself liquefying；After the low pressure CMR come out from CMR exchanger base returns to the suction port of compressor CMR surge tank
It is recycled.
Compared with prior art, the positive effect of the present invention is:
The present invention shares every grade of cooling load based on three circulations, natural gas successively pass through 1 plate-fin heat exchanger and
2 wound tube heat exchangers are cooled down, until liquefaction supercooling, process equipment quantity is few, and natural gas liquefaction device scale can reach
To single-row 600~8,000,000 tons/year；Cooling capacity needed for liquefaction process is by propane, WMR azeotrope, CMR azeotrope three
System provides, and system regulating measure is abundant, can provide matched cooling capacity for gas deliquescence process, flexible operation and fits to raw material
Answering property is good.Compared with prior art, it has a characteristic that
1, the present invention be the innovation that is carried out on the basis of multistage one pack system liquefaction process (MSC technique) cases of engineering and
It improves, there is technology continuity to have the advantages that compared with MSC technique
1) using propylene pre-cooling+ethylene cooling+azeotrope liquefaction to be subcooled in MSC technique, (azeotrope is with methane, nitrogen
Based on).Pre-cooling cycle uses propane in the present invention, and cooling cycle uses azeotrope, based on ethane, including methane and third
Alkane；The SAPMAC method cryogen that liquefied uses azeotrope, including nitrogen, methane, ethane.
2) cooling section, liquefaction super cooled sect are all made of azeotrope, adjust each refrigeration in combination with the optional type of driving equipment and follow
Ring load, neatly adjusts natural air cooling, liquefaction and supercooling temperature, and operational suitability is more preferable.
3) propylene and ethylene refrigeration system are exchanged heat using shell-and-tube heat exchanger or CIK heat exchanger in MSC technique, methane
Refrigeration cycle uses plate-fin heat exchanger；Propane pre-cooling section heat exchange equipment uses efficient plate-fin heat exchanger in the present invention, changes
Hot systems integrated level is high, has the advantages such as process flow is simplified, land occupation is few；The main cryogenic heat exchanger of WMR and CMR uses in the present invention
Wound tube heat exchanger, wound tube heat exchanger have the characteristics that separate unit heat exchange area is big, it is big to be advantageously implemented natural gas liquefaction device
Type.
2, double azeotrope liquefaction process (DMR technique) realize natural gas pre-cooling, liquid using 2 grades of azeotrope refrigeration cycle
Change and be subcooled, compared with DMR technique, the present invention shares liquefaction loads at different levels using three circularly coolings, realizes single-row 600~800
Ten thousand tons/year of ultra-large natural gas liquefaction device construction.
3, MFC technique is a kind of three circularly cooling circulation technologies, and it is cold that precooling zone, liquefaction stages, super cooled sect are all made of mixing
Agent refrigeration；Precooling zone of the present invention is pure C alkane cryogen compared with MFC.
4, AP-X is also a kind of three circularly cooling circulation technologies, and precooling zone is using propane refrigeration, liquefaction stages using mixing
Cryogen refrigeration, super cooled sect use nitrogen swell refrigeration；With AP-X technics comparing, super cooled sect of the present invention is freezed using azeotrope.
5, WMR throttling of the present invention, CMR throttling and high pressure LNG throttling are all made of liquid turbo-expander, liquid turbine expansion
Machine is constant entropy expansion, and compared with conventional throttle valves isenthalpic expansion, expansion efficiency is high, and LNG product yield can be improved 1~3%, unit
LNG product energy consumption reduces by 1~3%.
Detailed description of the invention
Examples of the present invention will be described by way of reference to the accompanying drawings, in which:
Fig. 1 is process flow chart of the invention.
Specific embodiment
It is a kind of to recycle natural gas liquefaction devices suitable for ultra-large three, as shown in Figure 1, comprising: propane pre-cooling plate wing
Formula heat exchanger 1, WMR wound tube heat exchanger 2, CMR wound tube heat exchanger 3, LNG hydraulic turbine expanding machine 4, LNG flash tank 5, LNG
Booster pump 6, propane compressor 7, propane compressor export cooler 8, the first high pressure propane throttle valve 9, the second high pressure propane section
It is pressed in stream valve 10, high pressure propane knockout drum 11, first in propane throttle valve 12, second and presses propane throttle valve 13, middle pressure third
Alkane gas-liquid liquid separation tank 14, low-pressure propane throttle valve 15, low-pressure propane gas-liquid liquid separation tank 16, the suction port of compressor WMR surge tank 17,
WMR compressor 18, WMR compressor outlet cooler 19, WMR hydraulic turbine expanding machine 20, the suction port of compressor CMR surge tank 21,
CMR compressor 22, CMR compressor outlet cooler 23, CMR hydraulic turbine expanding machine 24, in which:
Propane pre-cooling plate-fin heat exchanger 1, WMR wound tube heat exchanger 2, CMR wound tube heat exchanger 3, LNG hydraulic turbine are swollen
Swollen machine 4, LNG flash tank 5, LNG booster pump 6 are sequentially connected.
Propane compressor 7, propane compressor export cooler 8, the first high pressure propane throttle valve 9, propane pre-cooling plate-fin
Heat exchanger 1,7 high pressure suction inlet of propane compressor are sequentially connected；
Propane compressor exports cooler 8, the second high pressure propane throttle valve 10, high pressure propane knockout drum 11, first
Middle pressure propane throttle valve 12, propane pre-cooling plate-fin heat exchanger 1, pressure suction inlet is sequentially connected in propane compressor 7；
Propane throttle valve 13, middle pressure propane knockout drum 14, low pressure third are pressed in high pressure propane knockout drum 11, second
Alkane throttle valve 15, propane pre-cooling plate-fin heat exchanger 1, low-pressure propane knockout drum 16,7 low pressure suction port of propane compressor according to
It is secondary to be connected；
High pressure propane knockout drum 11 exports gas phase and is connected with 7 high pressure suction line of propane compressor；Middle pressure propane flammable gas
14 gaseous phase outlet of liquid knockout drum presses suction line to be connected with propane compressor 7.
The suction port of compressor WMR surge tank 17, WMR compressor 18, WMR compressor outlet cooler 19, propane pre-cooling plate wing
Formula heat exchanger 1, WMR wound tube heat exchanger 2, WMR hydraulic turbine expanding machine 20 are sequentially connected.
The suction port of compressor CMR surge tank 21, CMR compressor 22, CMR compressor outlet cooler 23, propane pre-cooling plate wing
Formula heat exchanger 1, WMR wound tube heat exchanger 2, CMR wound tube heat exchanger 3, CMR hydraulic turbine expanding machine 24 are sequentially connected.
The present invention also provides a kind of suitable for three ultra-large circulation natural gas liquefactions, includes the following steps:
1) propane precooling system is cooled to -30 DEG C~-39 DEG C to natural gas, WMR and CMR in advance:
From propane compressor 7 be pressurized to the propane of 1.5MPa.a~2.5MPa.a through propane cooler 8 be cooled to 20 DEG C~
50 DEG C, it is divided into 2 strands, wherein one liquid phase propane (about 15%~25%) is throttled by the first high pressure propane throttle valve 9, pressure drop
Enter propane pre-cooling plate-fin heat exchanger 1 after to 0.3MPa.a~0.6MPa.a, natural gas, WMR cryogen and CMR cryogen are carried out
Cooling (20 DEG C~0 DEG C), the phase propane come out from plate-fin heat exchanger 1 return to 7 high pressure suction inlet of propane compressor；Another stock
Liquid phase propane (75%~85%) is throttled by the second high pressure propane throttle valve 10, after pressure is down to 0.3MPa.a~0.6MPa.a
Gas-liquid separation is carried out into high pressure propane knockout drum 11, tank deck phase propane returns to 7 high pressure suction inlet of propane compressor；
The liquid phase of high pressure propane knockout drum 11 is divided into 2 strands, and wherein one liquid phase propane (45%~55%) passes through the
Propane throttle valve 12 is pressed to throttle in one, pressure enters propane pre-cooling plate-fin heat exchanger after being down to 0.2MPa.a~0.35MPa.a
1, cooling (- 10 DEG C~-20 DEG C) are carried out to natural gas, WMR cryogen and CMR cryogen, the gas phase third come out from plate-fin heat exchanger
Alkane returns in propane compressor 7 and presses suction inlet；Another burst of liquid phase propane (45%~55%), which passes through, presses propane throttle valve in second
13 throttlings, pressure is down to after 0.2MPa.a~0.35MPa.a enter in pressure propane knockout drum 14 carry out gas-liquid separation, tank deck
Phase propane returns in propane compressor 7 and presses suction inlet；
The liquid phase of middle pressure propane knockout drum 14 is throttled by throttle valve 15, and pressure is down to 0.1MPa.a~0.2MPa.a
Enter propane pre-cooling plate-fin heat exchanger 1 afterwards, cooling (- 30 DEG C~-39 DEG C) carried out to natural gas, WMR cryogen and CMR cryogen,
The phase propane come out from propane pre-cooling plate-fin heat exchanger 1 returns to propane compressor after low-pressure propane knockout drum 16
7 low pressure suction ports；
Low-pressure propane, middle pressure propane, high pressure propane are recycled after the pressurization of propane compressor 7.
2) natural gas, CMR cryogen are cooled to -65 DEG C~-95 DEG C by WMR refrigeration system:
The WMR cryogen come out from 2 bottom of WMR wound tube heat exchanger enters the suction port of compressor WMR surge tank 17, presses through WMR
Contracting machine 18 is pressurized to after 3MPa.a~5MPa.a and is cooled to 20 DEG C~50 DEG C through WMR cooler 19, into propane pre-cooling plate-fin
Heat exchanger 1 is cooled to -30 DEG C~-39 DEG C and liquefies；Liquid WMR enters WMR wound tube heat exchanger 2 and is cooled further to -65 DEG C
~-95 DEG C come out from top, after WMR fluid power expanding machine 20 is expanded to 0.2MPa.a~0.5MPa.a (- 70 DEG C~-100 DEG C)
WMR wound tube heat exchanger 2 is entered back into, cooling (- 65 DEG C~-95 DEG C) are carried out to natural gas, WMR cryogen and CMR cryogen；From WMR
The low pressure WMR (0.2MPa.a~0.5MPa.a, -35 DEG C~-45 DEG C) that 2 bottom of wound tube heat exchanger comes out returns to WMR compressor
It is recycled after inlet buffer 17.
3) CMR refrigeration system is natural gas and CMR cryogen all liquefies and supercooling provides cooling capacity:
CMR cryogen as CMR refrigeration system refrigerant passes through after CMR compressor 22 is pressurized to 5MPa.a~8MPa.a
CMR compressor outlet cooler 23 is cooled to 20 DEG C~50 DEG C, is cooled to -30 DEG C~-39 through propane pre-cooling plate-fin heat exchanger 1
DEG C, be cooled to-65 DEG C~-95 DEG C through WMR wound tube heat exchanger 2, be cooled in CMR wound tube heat exchanger 3-155 DEG C~-
It is come out after 160 DEG C from top, then enters back into CMR around pipe after CMR fluid power expanding machine 24 is expanded to 0.2MPa.a~0.5MPa.a
Formula heat exchanger 3 provides cooling capacity for natural gas and itself liquefaction supercooling；The low pressure CMR come out from 3 bottom of CMR wound tube heat exchanger
(0.2MPa.a~0.5MPa.a, -75 DEG C~-95 DEG C) is recycled after returning to the suction port of compressor CMR surge tank 21.
4) high pressure LNG expansion flash distillation
The natural gas come out at the top of CMR wound tube heat exchanger 3, which has liquefied and crossed, is cooled to -155 DEG C~-160 DEG C, after supercooling
Natural gas through LNG hydraulic turbine expanding machine 4 be expanded to (120kPa.a, -160 DEG C~-163 DEG C) afterwards enter LNG flash tank 5 in
Flash distillation, the BOG flashed off are sent to downstream BOG supercharging device, 5 tank bottom LNG of LNG flash tank sent after defeated 6 pressurization of LNG booster pump to
LNG storage unit.
The azeotrope WMR matches a certain amount of methane and propane based on ethane, and wherein methane volumetric content is
5%~15%, ethane is 70%~85%, and propane is 10%~20%；Azeotrope CMR group becomes nitrogen, methane, ethane,
Wherein nitrogen volume content is 10%~25%, ethane is 40%~65%, and propane is 30%~45%.
The working principle of the invention is:
The three circulation liquefaction systems provided by the invention based on high-efficiency appliance are applicable to single-row annual capacity up to 600~800
Ten thousand tons/year of ultra-large natural gas liquefaction devices, use three-level refrigeration cycle, and precooling zone uses propane cryogen, liquefaction and mistake
Cold section uses azeotrope；Pre-cooling cycle, liquefaction and cross SAPMAC method be respectively adopted a set of compression, cooling, condensation, turbine expansion and
Heat transfer process.
Hydraulic turbine expanding machine is selected in WMR, CMR and LNG throttling expansion in the present invention, and principle is constant entropy expansion, refrigeration
It is more efficient；It is recovered energy using hydraulic turbine expanding machine, for generating electricity, to reduce comprehensive energy consumption.
The present invention have the effect that 1) can according to project construction environment and unstripped gas condition variation, reasonable disposition
The composition and proportion of azeotrope, to optimize cooling and condensing temperature, so that the energy consumption of entire process system is minimum, area is suitable
Ying Xingguang；2) three-level refrigeration cycle, using efficient plate-fin heat exchanger and wound tube heat exchanger, heat exchange efficiency is high, can be reasonable
Cooling loads at different levels are shared, realize the enlargement of single line LNG device.3) WMR cryogen, the throttling of CMR cryogen are expanded using hydraulic turbine
Machine, high cooling efficiency, unit LNG product energy consumption are lower；4) high pressure LNG throttling uses hydraulic turbine expanding machine, and throttle effect is good,
Liquefied rate is higher.
Claims (10)
1. a kind of suitable for ultra-large three circulations natural gas liquefaction devices, it is characterised in that: including natural gas liquefaction pipeline,
The propane pre-cooling circulatory system, WMR cooling cycle system and CMR cooling cycle system, in which:
The natural gas liquefaction pipeline by propane heat exchanger, WMR heat exchanger, CMR heat exchanger, LNG expanding machine, LNG flash tank and
LNG booster pump is sequentially connected composition；
The propane pre-cooling circulatory system includes propane heat exchanger, propane compressor, propane compressor outlet cooler, high pressure third
Alkane knockout drum, middle pressure propane gas-liquid liquid separation tank and low-pressure propane knockout drum, for natural gas, WMR cryogen and CMR
Cryogen is pre-chilled；
The WMR cooling cycle system includes WMR heat exchanger, the suction port of compressor WMR surge tank, WMR compressor, WMR compressor
Cooler and WMR expanding machine are exported, for the further cooling and partial liquefaction of natural gas, CMR cryogen；
The CMR cooling cycle system includes CMR heat exchanger, the suction port of compressor CMR surge tank, CMR compressor, CMR compressor
Cooler and CMR expanding machine are exported, for providing cooling capacity for natural gas and CMR cryogen whole liquefaction and supercooling.
2. according to claim 1 a kind of suitable for three ultra-large circulation natural gas liquefaction devices, it is characterised in that:
In the propane pre-cooling circulatory system, propane compressor, propane compressor export cooler, the first high pressure propane throttle valve, third
Alkane heat exchanger and propane compressor high pressure suction inlet are sequentially connected；Propane compressor exports cooler, the throttling of the second high pressure propane
Valve, high pressure propane knockout drum, propane throttle valve, propane heat exchanger are pressed in first, pressure suction inlet is successively in propane compressor
It is connected；High pressure propane knockout drum, press in second propane throttle valve, middle pressure propane knockout drum, low-pressure propane throttle valve,
Propane heat exchanger, low-pressure propane knockout drum, propane compressor low pressure suction port are sequentially connected；High pressure propane knockout drum
Outlet gas phase is connected with propane compressor high pressure suction line；In middle pressure propane knockout drum gaseous phase outlet and propane compressor
Suction line is pressed to be connected.
3. according to claim 1 a kind of suitable for three ultra-large circulation natural gas liquefaction devices, it is characterised in that:
In the WMR cooling cycle system, WMR heat exchanger, the suction port of compressor WMR surge tank, WMR compressor, WMR compressor outlet are cold
But device, propane heat exchanger, WMR heat exchanger, WMR expanding machine, WMR heat exchanger are sequentially connected.
4. according to claim 1 a kind of suitable for three ultra-large circulation natural gas liquefaction devices, it is characterised in that:
In the CMR cooling cycle system, CMR heat exchanger, the suction port of compressor CMR surge tank, CMR compressor, CMR compressor outlet are cold
But device, propane heat exchanger, WMR heat exchanger, CMR heat exchanger, CMR expanding machine, CMR heat exchanger are sequentially connected.
5. according to claim 1 to a kind of natural suitable for three ultra-large circulations described in any claim requirement in 4
Gas liquefaction device, it is characterised in that: the LNG expanding machine, WMR expanding machine and CMR expanding machine are hydraulic turbine expanding machine.
6. according to claim 5 a kind of suitable for three ultra-large circulation natural gas liquefaction devices, it is characterised in that:
The propane heat exchanger is plate-fin heat exchanger, and the WMR heat exchanger and CMR heat exchanger are wound tube heat exchanger.
7. a kind of suitable for three ultra-large circulation natural gas liquefactions, characterized by the following steps:
1) propane cycles system is natural gas, WMR cryogen and the pre-cooling of CMR cryogen provide cooling capacity:
The propane being pressurized from propane compressor is divided into two strands after propane cooler is cooling, and wherein one liquid phase propane passes through first
Enter propane heat exchanger after high pressure propane throttle valve reducing pressure by regulating flow power, is provided for the cooling of natural gas, WMR cryogen and CMR cryogen cold
Amount, the phase propane come out from propane heat exchanger return to propane compressor high pressure suction inlet；Another strand of liquid phase propane passes through second
Enter high pressure propane knockout drum after high pressure propane throttle valve reducing pressure by regulating flow power and carry out gas-liquid separation, in which: tank deck gas phase third
Alkane returns to propane compressor high pressure suction inlet, and tank bottom liquid phase is divided into two strands, and wherein one liquid phase propane, which passes through in first, presses propane
Enter propane heat exchanger after throttle valve reducing pressure by regulating flow power, continues cooling for natural gas, WMR cryogen and CMR cryogen and cooling capacity is provided, from
The phase propane that propane heat exchanger comes out, which returns to, presses suction inlet in propane compressor；Another strand of liquid phase propane, which passes through in second, presses third
Propane knockout drum is pressed to carry out gas-liquid separation in entering after alkane throttle valve reducing pressure by regulating flow power, tank deck phase propane returns to propane pressure
Suction inlet is pressed in contracting machine, the liquid phase propane of tank bottom is by entering propane heat exchanger after low-pressure propane throttle valve reducing pressure by regulating flow power
Natural gas, WMR cryogen and CMR cryogen continue cooling offer cooling capacity, and the phase propane come out from propane heat exchanger passes through low pressure third
Propane compressor low pressure suction port is returned to after alkane knockout drum；Low-pressure propane, middle pressure propane, high pressure propane are through propane compressor
It is recycled after pressurization；
2) WMR refrigeration system is natural gas, further cooling and partial liquefaction provides cooling capacity to CMR cryogen:
The WMR cryogen come out from WMR exchanger base enters the suction port of compressor WMR surge tank, through WMR compressor boost and passes through
After WMR cooler is cooling, into cooling liquid in propane heat exchanger；Liquid WMR enters after WMR heat exchanger further cools down from top
Portion comes out, and WMR heat exchanger is entered back into after WMR expander to low pressure, is that natural gas, WMR cryogen and CMR cryogen are further
Cooling and partial liquefaction provides cooling capacity；The low pressure WMR cryogen come out from WMR exchanger base returns to the suction port of compressor WMR and buffers
It is recycled after tank；
3) CMR refrigeration system is natural gas and CMR cryogen all liquefies and supercooling provides cooling capacity:
CMR cryogen is successively cold through CMR cooler, propane heat exchanger, WMR heat exchanger, CMR heat exchanger after CMR compressor boost
But it is come out at the top of CMR heat exchanger after, then enters back into CMR heat exchanger after CMR expander to low pressure, for natural gas and certainly
Body liquefaction supercooling provides cooling capacity；The low pressure CMR come out from CMR exchanger base is carried out after returning to the suction port of compressor CMR surge tank
Circulation.
8. according to claim 7 a kind of suitable for three ultra-large circulation natural gas liquefactions, it is characterised in that:
The group of the WMR cryogen becomes methane, ethane and propane, wherein methane volumetric content be 5%~15%, ethane be 70%~
85%, propane is 10%~20%.
9. according to claim 7 a kind of suitable for three ultra-large circulation natural gas liquefactions, it is characterised in that:
The group of the CMR cryogen becomes nitrogen, methane, ethane, wherein nitrogen volume content be 10%~25%, ethane be 40%~
65%, propane is 30%~45%.
10. according to claim 7 a kind of suitable for three ultra-large circulation natural gas liquefactions, feature exists
In: the liquefaction and mistake that come out at the top of CMR heat exchanger are cooled to -155 DEG C~-160 DEG C of natural gas, extremely through LNG expander
120kPa.a, which enters in LNG flash tank, to be flashed, and the BOG flashed off is sent to downstream BOG supercharging device, and tank bottom LNG is through LNG booster pump
It is sent after defeated pressurization to LNG storage unit.
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| PCT/CN2019/096445 WO2020248328A1 (en) | 2019-06-11 | 2019-07-18 | Three-cycle natural gas liquefaction apparatus and method suitable for ultra-large scale |
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| CN112009697A (en) * | 2020-09-02 | 2020-12-01 | 成都精智艺科技有限责任公司 | Efficient LNG ship power supply system and method |
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