CN105651001B - Liquefaction system suitable for different temperatures methane gas and the method using the system liquefied methane gas - Google Patents
Liquefaction system suitable for different temperatures methane gas and the method using the system liquefied methane gas Download PDFInfo
- Publication number
- CN105651001B CN105651001B CN201610105153.1A CN201610105153A CN105651001B CN 105651001 B CN105651001 B CN 105651001B CN 201610105153 A CN201610105153 A CN 201610105153A CN 105651001 B CN105651001 B CN 105651001B
- Authority
- CN
- China
- Prior art keywords
- methane gas
- cryogen
- import
- heat exchanger
- outlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 636
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000007788 liquid Substances 0.000 claims abstract description 222
- 230000008676 import Effects 0.000 claims abstract description 168
- 239000003507 refrigerant Substances 0.000 claims abstract description 88
- 238000003860 storage Methods 0.000 claims abstract description 23
- 239000007789 gas Substances 0.000 claims description 312
- 230000006835 compression Effects 0.000 claims description 90
- 238000007906 compression Methods 0.000 claims description 90
- 238000001816 cooling Methods 0.000 claims description 17
- 239000003795 chemical substances by application Substances 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 12
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 10
- QWTDNUCVQCZILF-UHFFFAOYSA-N isopentane Chemical compound CCC(C)C QWTDNUCVQCZILF-UHFFFAOYSA-N 0.000 claims description 10
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 9
- 239000007791 liquid phase Substances 0.000 claims description 7
- 229910052757 nitrogen Inorganic materials 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 5
- AFABGHUZZDYHJO-UHFFFAOYSA-N dimethyl butane Natural products CCCC(C)C AFABGHUZZDYHJO-UHFFFAOYSA-N 0.000 claims description 5
- 239000001294 propane Substances 0.000 claims description 5
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 4
- 239000005977 Ethylene Substances 0.000 claims description 4
- 230000001737 promoting effect Effects 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 21
- 239000000110 cooling liquid Substances 0.000 abstract description 14
- 238000001704 evaporation Methods 0.000 abstract description 12
- 230000008020 evaporation Effects 0.000 abstract description 12
- 238000004781 supercooling Methods 0.000 abstract 1
- 230000008569 process Effects 0.000 description 15
- 230000008901 benefit Effects 0.000 description 13
- 238000005057 refrigeration Methods 0.000 description 10
- 239000000203 mixture Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 4
- 235000013399 edible fruits Nutrition 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000006837 decompression Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- 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
- F25J1/0047—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
-
- 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
- F25J1/0212—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 a single flow MCR cycle
-
- 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
- F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
-
- 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
-
- 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.
- F25J1/0291—Refrigerant compression by combined gas compression and liquid pumping
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/06—Splitting of the feed stream, e.g. for treating or cooling in different ways
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
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
Method the invention discloses the liquefaction system suitable for different temperatures methane gas and using the system liquefied methane gas, system include：Connected methane gas storage tank, heat exchanger, stage compressor, level-one cooler, knockout drum, split-compressor, secondary coolers and distributor, first methane gas import, first liquid state cryogen import and the outlet of the first gaseous state cryogen are arranged on heat exchanger front end, second methane gas import is arranged in the middle part of heat exchanger, second liquid state cryogen import and the outlet of the second liquid refrigerant are arranged on the end of heat exchanger, control valve is set respectively on methane gas storage tank and the methane gas conveying pipe of the first methane gas import and the second methane gas import, second liquid state cryogen import is connected by cryogen pipeline with the outlet of the second liquid refrigerant.The system can realize that cryogen evaporation curve matches to greatest extent with methane gas cooling liquid supercooling curve in heat exchanger at a temperature of different methane gas, so as to improve methane gas liquefaction efficiency and reduce liquefaction energy consumption.
Description
Technical field
The invention belongs to chemical technology field, specifically, the present invention relates to a kind of suitable for different temperatures methane gas
Liquefaction system and the method using the system liquefied methane gas.
Background technology
Be continuously increased with the growth of China's economic and to energy demand, and with China to environmental improvement increasingly
Pay attention to and increase input, Chinese clean energy resource such as methane gas dosage increases sharply.However methane gas is not easy to transport and store,
To meet the civilian demand of growing industrial or agricultural, a kind of easily transport and storage side of the liquefied methane gas as methane gas
Formula, demand increase year by year.Recent years, the growth of domestic methane gas demand promote the quick hair of liquefied methane gas industry
Exhibition, successively has some liquefied methane gas factories to be constructed and put into operation.
Methane gas liquefaction process is broadly divided into following three kinds both at home and abroad at present：
1) cascade refrigeration cycles；2) azeotrope refrigeration cycle, but can be subdivided into liquefying plant in itself band precooling or without
The single-stage mixing cryogen Xun Huan of precooling and multistage azeotrope cycle；3) swell refrigeration, and liquefying plant band in itself can be subdivided into
Precooling or without precooling single-stage expansion refrigeration and multiple expansion freeze.
Methane gas liquefaction process with swell refrigeration Xun Huan is because plant energy consumption is excessively high, in recent years gradually by single-stage mixing cryogen
Refrigerating cycle liquefied technical substitution.
Single-stage mixing cryogen refrigerating cycle liquefied technique is the prevailing technology of domestic and international methane gas liquefying plant at present.And liquid
The mixing cryogen refrigerating cycle liquefied process liquefaction flow of multistage for carrying propane pre-cooling in itself is put in makeup, and it is basic to be chiefly used in ultra-large type
Load type methane gas liquefying plant.Stage refrigerating cycle liquefaction process is used since flow sheet equipment is more, flow is complicated, investment is big
It is less.
Single-stage mixing cryogen refrigeration cycle also has its shortcoming：In the actual production process, it is whole when unstripped gas temperature change
The cold that a required cold of liquefaction process is provided with cryogen is difficult to accomplish to exactly match, and heat exchange efficiency is caused to decline, power consumption
Increase.Therefore liquefying plant need to increase chilldown system, then need to increase precooling refrigeration cycle, including precooling refrigeration compressor, precooling
Heat exchanger, precooling refrigerant preparation system and recovery system etc..
According to the characteristics of methane gas liquefying plant front end, using the existing methane gas precooling technological process of fore device and set
It is standby, it can be to avoid the chilldown system of methane gas liquefying plant in itself be increased, while the investment of methane gas liquefying plant is reduced, again
Can reduce the energy consumption of liquefying plant in itself, such methane liquefaction technology in current industrial production not yet.
The content of the invention
It is contemplated that it solves at least some of the technical problems in related technologies.For this purpose, the present invention
One purpose is to propose a kind of liquefaction system suitable for different temperatures methane gas and utilizes the system liquefied methane gas
Method, the system can realize that the cooling liquid of the evaporation curve of cryogen and methane gas in heat exchanger at a temperature of different methane gas is bent
Line matches to greatest extent, so as to realize the maximization of heat exchanger heat exchange efficiency, and then improves the liquefaction efficiency of methane gas,
And have the advantages that low energy consumption, variable working condition ability is strong, technological process is simple and investment is low.
In one aspect of the invention, the present invention proposes a kind of liquefaction system suitable for different temperatures methane gas.Root
According to the embodiment of the present invention, which includes：
Methane gas storage tank；
Heat exchanger, the heat exchanger have the first methane gas import, the second methane gas import, the first liquid state cryogen into
Mouth, the second liquid state cryogen import, the outlet of the first gaseous state cryogen, the outlet of the second liquid refrigerant and liquefied methane gas outlet, it is described
First methane gas import, the first liquid state cryogen import and the first gaseous state cryogen outlet are arranged on the heat exchanger
Front end, the second methane gas import is arranged in the middle part of the heat exchanger, the second liquid state cryogen import and described second
Liquid refrigerant exports the end for being arranged on the heat exchanger, the first methane gas import and the second methane gas import difference
It is connected with the methane gas storage tank, and in the methane gas storage tank and the first methane gas import and second methane gas
The first control valve and the second control valve, the second liquid state cryogen import are respectively arranged on the methane gas conveying pipe of import
It is connected by cryogen pipeline with second liquid refrigerant outlet, throttle valve is provided on the cryogen pipeline；
Stage compressor, there is the stage compressor the 3rd gaseous state cryogen import and one stage of compression cryogen to export, described
3rd gaseous state cryogen import is connected with the first gaseous state cryogen outlet；
There is the import of one stage of compression cryogen and azeotrope to export for level-one cooler, the level-one cooler, the level-one
Compression cryogen import is connected with one stage of compression cryogen outlet；
Knockout drum, the knockout drum have azeotrope import, the outlet of the 4th gaseous state cryogen and the 4th liquid
Cryogen exports, and the azeotrope import is connected with azeotrope outlet；
Split-compressor, there is the split-compressor the 4th gaseous state cryogen import and two-stage compression cryogen to export, described
4th gaseous state cryogen import is connected with the 4th gaseous state cryogen outlet；
There is the import of two-stage compression cryogen and the 5th liquid state cryogen to export for secondary coolers, the secondary coolers, institute
The import of two-stage compression cryogen is stated with two-stage compression cryogen outlet to be connected；
Distributor, the distributor have the 4th liquid refrigerant import, the 5th liquid state cryogen import, liquid refrigerant outlet
It is exported with gaseous state cryogen, the 4th liquid refrigerant import is connected with the 4th liquid refrigerant outlet, the 5th liquid state
The outlet of cryogen import and the 5th liquid state cryogen is connected, the gaseous state cryogen outlet and the liquid refrigerant export respectively with
The first liquid state cryogen import is connected.
As a result, the liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention by heat exchanger not
With two methane gas imports of setting on position, and on the methane gas conveying pipe between methane gas storage tank and methane gas import
Control valve is set respectively, it can be according to the feeding temperature adjusting control valve of methane gas, so as to the methane to two methane gas imports
Throughput is adjusted so that the cooling liquid of the evaporation curve of cryogen and methane gas is bent in heat exchanger at a temperature of different methane gas
Line matches to greatest extent, and then can realize the maximization of heat exchanger heat exchange efficiency, and then improves the liquefaction efficiency of methane gas,
And have the advantages that low energy consumption, variable working condition ability is strong, technological process is simple and investment is low, while using the throttling of cryogen single
Single-cycle technique, short flow in ice chest, number of devices is few, characteristics of compact layout, compared with traditional multistage cooling liquid flow, subtracts
Cryo Equipment, instrument and pipeline in few ice chest, reduce ice chest size, 30% investment are at least saved than traditional handicraft, and is freezed
Power consumption of circulation and compression is relatively low, and main heat exchanger and ice chest size are small, be conducive to key equipment production domesticization and liquefying plant it is big
Type.
In addition, the liquefaction system according to the above embodiment of the present invention suitable for different temperatures methane gas can also have such as
Under additional technical characteristic：
In some embodiments of the invention, the heat exchanger includes first cold heat exchanger and whole cold heat exchanger, described just cold
Cryogen import, the outlet of first liquid state cryogen and first cold methane gas export after heat exchanger has heat exchange, and the end cold heat exchanger has
Cryogen outlet and just cold methane gas import after first liquid state cryogen import, heat exchange, cryogen import and the heat exchange after the heat exchange
Cryogen outlet afterwards is connected, and the just liquid state cryogen outlet is connected with the just liquid state cryogen import, the just cold methane gas
Outlet and the second methane gas import are connected respectively with the just cold methane gas import, and the first methane gas import,
The first liquid state cryogen import and the first gaseous state cryogen outlet are arranged on the just cold heat exchanger, second gas
Liquid refrigerant import and second liquid refrigerant outlet are arranged on the whole cold heat exchanger.Thus, it is possible to significantly improve first
The heat exchange efficiency of alkane gas and cryogen, so as to improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, by adjusting the aperture of first control valve and second control valve,
The mixing temperature for controlling just cold methane gas and the second methane gas is -30~-70 degrees Celsius.
In some embodiments of the invention, when the mixing temperature is less than -70 degrees Celsius, first control is turned down
Valve tunes up second control valve thus, it is possible to further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, when the mixing temperature is higher than -30 degrees Celsius, first control is tuned up
Valve turns second control valve down.Thus, it is possible to further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the system further comprises：Surge tank, the surge tank respectively with it is described
The outlet of first gaseous state cryogen is connected with the 3rd gaseous state cryogen import；Liquid phase pump, the liquid phase pump respectively with the 4th liquid
The outlet of state cryogen is connected with the 4th liquid refrigerant import.Thus, it is possible to significantly improve the operation stability of liquefaction system.
In the second aspect of the invention, the present invention proposes a kind of method of liquefied methane gas.Reality according to the present invention
Example is applied, this method is carried out using the liquefaction system suitable for different temperatures methane gas described above.It is according to the present invention
Specific embodiment, this method include：
Methane gas is supplied, heat exchange processing is carried out into the heat exchanger, so that the methane gas and the first liquid state
Cryogen carries out heat exchange processing, to obtain the first gaseous state cryogen and liquefied methane gas；
The first gaseous state cryogen is supplied into the stage compressor and carries out one stage of compression processing, to obtain level-one
Compress cryogen；
The one stage of compression cryogen is supplied into the level-one cooler and carries out level-one cooling treatment, to be mixed
Cryogen；
The azeotrope is supplied, separating treatment is carried out into the knockout drum, to obtain the 4th gaseous state cryogen
With the 4th liquid refrigerant；
The 4th gaseous state cryogen is supplied into the split-compressor and carries out two-stage compression processing, to obtain two level
Compress cryogen；
The two-stage compression cryogen is supplied into the secondary coolers and carries out two level cooling treatment, to obtain the 5th
Liquid state cryogen；
4th liquid refrigerant and the 5th liquid state cryogen are supplied into the distributor and mix laggard promoting the circulation of qi
Liquid separates, and to obtain liquid refrigerant and gaseous state cryogen, and the gaseous state cryogen and the liquid refrigerant is respectively fed to institute
Heat exchanger is stated to use as the first liquid state cryogen.
The method of liquefied methane gas according to embodiments of the present invention is suitable for different temperatures methane by using above-mentioned as a result,
The liquefaction system of gas can realize the evaporation curve of cryogen and the cooling liquid of methane gas in heat exchanger at a temperature of different methane gas
Curve matches to greatest extent, so as to realize the maximization of heat exchanger heat exchange efficiency, and then improves the liquefaction effect of methane gas
Rate, and have the advantages that low energy consumption, variable working condition ability is strong, technological process is simple and investment is low.
In addition, the method for liquefied methane gas according to the above embodiment of the present invention can also have following additional technology spy
Sign：
In some embodiments of the invention, the heat exchange processing is carried out according to the following steps：The heat exchange processing
It is to be carried out according to the following steps：The first liquid state cryogen is supplied to the just cold heat exchanger, to obtain just gas-liquid
State cryogen；The just liquid state cryogen is supplied to the whole cold heat exchanger, to obtain the second liquid refrigerant；By described second
Liquid refrigerant is supplied to the throttle valve, to obtain whole liquid state cryogen；A part for the methane gas is supplied to described
Whole cold heat exchanger exchanges heat with the whole liquid state cryogen, so as to cryogen and liquefied methane gas after being exchanged heat；By the first
Another part of alkane gas is supplied to exchange heat into the just cold heat exchanger with cryogen after the heat exchange, to obtain just cold methane
Gas and the first gaseous state cryogen, and supplied after the just cold methane gas is mixed with a part for the methane gas to the end
It exchanges heat in cold heat exchanger with the whole liquid state cryogen.Thus, it is possible to the heat exchange efficiency of methane gas and cryogen is significantly improved,
So as to improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, by adjusting the aperture of first control valve and second control valve,
The mixing temperature for controlling the just cold methane gas and a part for the methane gas is -30~-70 degrees Celsius.
In some embodiments of the invention, when the mixing temperature is less than -70 degrees Celsius, first control is turned down
Valve tunes up second control valve, so that most of methane gas is supplied to the whole cold heat exchanger, fraction methane gas supplies
To extremely described just cold heat exchanger.Thus, it is possible to further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, when the mixing temperature is higher than -30 degrees Celsius, first control is tuned up
Valve turns second control valve down, so that most of methane gas is supplied to the just cold heat exchanger, fraction methane gas supplies
To extremely described whole cold heat exchanger.Thus, it is possible to further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the temperature of the just liquid state cryogen is -30~-70 degrees Celsius.As a result, may be used
To further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the temperature of second liquid refrigerant is -140~-165 degrees Celsius.As a result,
The liquefaction efficiency of methane gas can be further improved.
In some embodiments of the invention, the temperature of the whole liquid state cryogen is -145~-170 degrees Celsius, pressure
For 0.2~0.5MPa (A).Thus, it is possible to further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the temperature of the just cold methane gas is -30~-70 degrees Celsius.Thus, it is possible to
Further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the pressure of the one stage of compression cryogen is 1.0~2.0MPa (A).As a result, may be used
To further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the pressure of the two-stage compression cryogen is 2.5~5.0MPa (A).As a result, may be used
To further improve the liquefaction efficiency of methane gas.
In some embodiments of the invention, the first liquid state cryogen contains：The nitrogen of 5~10% parts by volume；20
The methane of~30% parts by volume；The ethylene of 25~35% parts by volume；The propane of 10~20% parts by volume；And 10~20% volume
The isopentane of part.Thus, it is possible to further improve the liquefaction efficiency of methane gas.
The additional aspect and advantage of the present invention will be set forth in part in the description, and will partly become from the following description
It obtains substantially or is recognized by the practice of the present invention.
Description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will become in the description from combination accompanying drawings below to embodiment
Substantially and it is readily appreciated that, wherein：
Fig. 1 is the structural representation of the liquefaction system according to an embodiment of the invention suitable for different temperatures methane gas
Figure；
Fig. 2 is the structural representation of the liquefaction system suitable for different temperatures methane gas of further embodiment according to the present invention
Figure；
Fig. 3 is the structural representation of the liquefaction system suitable for different temperatures methane gas of another embodiment according to the present invention
Figure；
Fig. 4 is the method flow schematic diagram of liquefied methane gas according to an embodiment of the invention；
Fig. 5 is the method flow schematic diagram of the liquefied methane gas of further embodiment according to the present invention.
Specific embodiment
The embodiment of the present invention is described below in detail, the example of the embodiment is shown in the drawings, wherein from beginning to end
Same or similar label represents same or similar element or has the function of same or like element.Below with reference to attached
The embodiment of figure description is exemplary, it is intended to for explaining the present invention, and is not considered as limiting the invention.
In the description of the present invention, it is to be understood that term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ",
" thickness ", " on ", " under ", "front", "rear", "left", "right", " vertical ", " level ", " top ", " bottom ", " interior ", " outer ", " up time
The orientation or position relationship of the instructions such as pin ", " counterclockwise ", " axial direction ", " radial direction ", " circumferential direction " be based on orientation shown in the drawings or
Position relationship is for only for ease of the description present invention and simplifies description rather than instruction or imply that signified device or element must
There must be specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.
In addition, term " first ", " second " are only used for description purpose, and it is not intended that instruction or hint relative importance
Or the implicit quantity for indicating indicated technical characteristic.Define " first " as a result, the feature of " second " can be expressed or
Implicitly include at least one this feature.In the description of the present invention, " multiple " are meant that at least two, such as two, three
It is a etc., unless otherwise specifically defined.
In the present invention, unless otherwise clearly defined and limited, term " installation ", " connected ", " connection ", " fixation " etc.
Term should be interpreted broadly, for example, it may be being fixedly connected or being detachably connected or integral；Can be that machinery connects
It connects or is electrically connected；It can be directly connected, can also be indirectly connected by intermediary, can be in two elements
The connection in portion or the interaction relationship of two elements, unless otherwise restricted clearly.For those of ordinary skill in the art
For, the concrete meaning of above-mentioned term in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature can be with "above" or "below" second feature
It is that the first and second features contact directly or the first and second features pass through intermediary mediate contact.Moreover, fisrt feature exists
Second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper or be merely representative of
Fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " lower section " and " below " can be
One feature is immediately below second feature or obliquely downward or is merely representative of fisrt feature level height less than second feature.
In one aspect of the invention, the present invention proposes a kind of liquefaction system suitable for different temperatures methane gas.Root
According to the embodiment of the present invention, which includes：Methane gas storage tank；Heat exchanger, the heat exchanger have the first methane gas import, the
The import of bismethane gas, the first liquid state cryogen import, the second liquid state cryogen import, the outlet of the first gaseous state cryogen, the second liquid
Cryogen exports and liquefied methane gas outlet, the first methane gas import, the first liquid state cryogen import and described first
Gaseous state cryogen exports the front end for being arranged on the heat exchanger, and the second methane gas import is arranged in the middle part of the heat exchanger, institute
It states the second liquid state cryogen import and second liquid refrigerant outlet is arranged on the end of the heat exchanger, first methane
Gas import and the second methane gas import are connected respectively with the methane gas storage tank, and in the methane gas storage tank and described
The first control valve and are respectively arranged on the methane gas conveying pipe of first methane gas import and the second methane gas import
Two control valves, the second liquid state cryogen import is connected by cryogen pipeline with second liquid refrigerant outlet, described cold
Throttle valve is provided on agent pipeline；Stage compressor, the stage compressor have the 3rd gaseous state cryogen import and one stage of compression
Cryogen exports, and the 3rd gaseous state cryogen import is connected with the first gaseous state cryogen outlet；Level-one cooler, the level-one are cold
But utensil has the import of one stage of compression cryogen and azeotrope outlet, the one stage of compression cryogen import and the one stage of compression cryogen
Outlet is connected；Knockout drum, the knockout drum have azeotrope import, the outlet of the 4th gaseous state cryogen and the 4th liquid
Cryogen exports, and the azeotrope import is connected with azeotrope outlet；Split-compressor, the split-compressor have
4th gaseous state cryogen import and the outlet of two-stage compression cryogen, the 4th gaseous state cryogen import are exported with the 4th gaseous state cryogen
It is connected；There is the import of two-stage compression cryogen and the 5th liquid state cryogen to export for secondary coolers, the secondary coolers, and described two
Grade compression cryogen import is connected with two-stage compression cryogen outlet；Distributor, the distributor have the 4th liquid refrigerant into
Mouth, the 5th liquid state cryogen import, liquid refrigerant outlet and the outlet of gaseous state cryogen, the 4th liquid refrigerant import and described the
The outlet of four liquid refrigerants is connected, and the 5th liquid state cryogen import is connected with the 5th liquid state cryogen outlet, the gas
State cryogen exports and liquid refrigerant outlet is connected respectively with the first liquid state cryogen import.Inventor has found, passes through
Two methane gas imports, and the methane between methane gas storage tank and methane gas import are set on the different position of heat exchanger
Letter shoot sets control valve respectively on road, can be according to the feeding temperature adjusting control valve of methane gas, so as to two methane
The methane gas flow of gas import is adjusted so that at a temperature of different methane gas in heat exchanger cryogen evaporation curve and methane gas
Cooling liquid curve match to greatest extent, and then can realize the maximization of heat exchanger heat exchange efficiency, and then improve methane
The liquefaction efficiency of gas, and have the advantages that low energy consumption, variable working condition ability is strong, technological process is simple and investment is low, it adopts simultaneously
It is throttled single-cycle technique with cryogen single, short flow in ice chest, number of devices is few, characteristics of compact layout, is cooled down with traditional multistage
Liquefaction flow path is compared, and reduces Cryo Equipment, instrument and pipeline in ice chest, is reduced ice chest size, is at least saved than traditional handicraft
30% investment, and refrigeration cycle compression power consumption is relatively low, and main heat exchanger and ice chest size are small, are conducive to the domestic of key equipment
Change and the enlargement of liquefying plant.
It is retouched in detail below with reference to the liquefaction system suitable for different temperatures methane gas of Fig. 1-3 pairs of embodiment of the present invention
It states.According to an embodiment of the invention, which includes：It is methane gas storage tank 100, heat exchanger 200, methane gas conveying pipe 300, cold
Agent pipeline 400, stage compressor 500, level-one cooler 600, knockout drum 700, split-compressor 800, secondary coolers
900 and distributor 1000.
According to an embodiment of the invention, methane gas storage tank 100 is suitable for storage methane gas.It should be noted that herein
" methane gas storage tank " can be any device in the prior art that can be used for storing methane gas.
According to an embodiment of the invention, there is the first methane gas import 201, the second methane gas import on heat exchanger 200
202nd, the first liquid state cryogen import 203, the second liquid state cryogen import 204, the first gaseous state cryogen export the 205, second liquid
Cryogen outlet 206 and liquefied methane gas outlet 207, the first methane gas import 201, the first liquid state cryogen import 203 and first
The front end that gaseous state cryogen outlet 205 is arranged on heat exchanger 200 (close to one end of methane gas storage tank i.e. on heat exchanger, is specifically changed
The temperature of hot device front end cryogen is -30~-70 degrees Celsius), the second methane gas import 202 is arranged in the middle part of heat exchanger, the second gas
204 and second liquid refrigerant of liquid refrigerant import outlet 206 is arranged on the end of heat exchanger 200, and (specific heat exchanger end is cold
The temperature of agent is -145~-170 degrees Celsius), the first methane gas import 201 and the second methane gas import 202 respectively with methane gas
Storage tank 100 is connected, and is adapted so that methane gas carries out heat exchange processing with the first liquid state cryogen, so as to obtain the first gaseous state
Cryogen and liquefied methane gas, gained liquefied methane gas are stored after decompression into liquefied pot.And in methane gas storage tank 100 and
The first control valve 11 is respectively arranged on the methane gas conveying pipe 300 of one methane gas import 201 and the second methane gas import 202
With the second control valve 12.Inventor has found, by setting two methane gas imports on the different position of heat exchanger, and in first
Control valve is set respectively on methane gas conveying pipe between alkane gas storage tank and methane gas import, it can be according to the charging of methane gas
Temperature adjusting control valve, so as to which the methane gas flow of two methane gas imports be adjusted so that at a temperature of different methane gas
The evaporation curve of cryogen matches to greatest extent with the cooling liquid curve of methane gas in heat exchanger, and then can realize heat exchanger
The maximization of heat exchange efficiency, and then improve the liquefaction efficiency of methane gas.It should be noted that " heat exchanger " herein is placed in
It is used in ice chest.
According to a particular embodiment of the invention, the second liquid state cryogen import 204 passes through 400 and second liquid of cryogen pipeline
Cryogen outlet 206 is connected, and throttle valve 13 is provided on cryogen pipeline 400.Inventor has found, by the way that throttle valve is set to depressurize
The temperature of second liquid refrigerant can be continued to 5~20 degrees Celsius of reduction, i.e., can provide the temperature difference by throttle valve takes the photograph for 5~20
The cold of family name's degree, so as to further improve the liquefaction efficiency of methane gas.
According to an embodiment of the invention, with reference to figure 2, heat exchanger 200 can include first cold heat exchanger 21 and whole cold heat exchanger
22。
According to a particular embodiment of the invention, first cold heat exchanger 21 has cryogen import 208, first liquid state cryogen after heat exchange
Outlet 209 and just cold methane gas outlet 210, and the first methane gas import 201, the first liquid state cryogen import 203 and first
Gaseous state cryogen outlet 205 is arranged on just cold heat exchanger 21.
According to a particular embodiment of the invention, whole cold heat exchanger 22 has cryogen after first liquid state cryogen import 211, heat exchange
Outlet 212 and first cold methane gas import 213, after heat exchange cryogen import 208 export 212 with cryogen after heat exchange and be connected, first liquid state
Cryogen outlet 209 is connected with first liquid state cryogen import 211, and just cold methane gas outlet 210 and the second methane gas import 202 is distinguished
It is connected with first cold methane gas import 213, and the second liquid state cryogen import 204 and the second liquid refrigerant outlet 206 are arranged on
On whole cold heat exchanger 22.
During being somebody's turn to do, specifically, supplying the first liquid state refrigerant gas to first cold heat exchanger, it is cold to obtain just liquid state
Agent；Then first liquid state cryogen is supplied to the whole cold heat exchanger, obtains the second liquid refrigerant；Then by the second liquid refrigerant
Supply obtains whole liquid state cryogen to throttle valve；Then by the part supply of methane gas to whole cold heat exchanger and whole liquid state
Cryogen exchanges heat, cryogen and liquefied methane gas after being exchanged heat；Then another part of methane gas is supplied to first cold heat exchange
It exchanges heat in device with cryogen after heat exchange, obtains just cold methane gas and the first gaseous state cryogen, and will first cold methane gas and methane gas
Part mixing after supply and exchanges heat into whole cold heat exchanger with whole liquid state cryogen, cryogen and the first that liquefies after exchange heat
Alkane gas.
A specific embodiment according to the present invention is made just cold by the aperture for adjusting the first control valve, the second control valve
The mixing temperature of methane gas and the second methane gas is at -30~-70 DEG C.When mixing temperature is less than -70 degrees Celsius, the first control is turned down
Valve tunes up the second control valve so that most of methane gas is supplied to whole cold heat exchanger, and fraction methane gas is supplied to first cold heat exchange
Device,
Another specific embodiment according to the present invention, originally the mixing temperature of cold methane gas and the second methane gas higher than-
At 30 degrees Celsius, the first control valve is tuned up, turns the second control valve down so that most of methane gas is supplied to first cold heat exchanger, small
Portion of methane gas is supplied to whole cold heat exchanger.As a result, by using the first cold heat exchanger being connected with each other and whole cold heat exchanger, and will
First methane gas import and the second methane gas import are separately positioned on just cold heat exchanger and whole cold heat exchanger, by being arranged on first
The first control valve and the second control valve on alkane letter shoot road can divide according to the feeding temperature adjusting control valve of methane gas
The other methane gas flow to entering first cold heat exchanger and whole cold heat exchanger is adjusted so that heat exchanger at a temperature of different methane gas
The evaporation curve of middle cryogen matches to greatest extent with the cooling liquid curve of methane gas, and then can realize heat exchanger heat exchange effect
The maximization of rate, and then the liquefaction efficiency of methane gas is improved, and with low energy consumption, variable working condition ability is strong, technological process is simple
And the low advantage of investment.
A specific embodiment according to the present invention, the temperature of first liquid state cryogen can be -30~-70 degrees Celsius.
Another specific embodiment according to the present invention, the temperature of the second liquid refrigerant can be -140~-165 Celsius
Degree.
Another specific embodiment according to the present invention, the temperature of whole liquid refrigerant can be -145~-170 degrees Celsius,
Pressure can be 0.2~0.5MPa (A).
Another specific embodiment according to the present invention, the temperature of first cold methane gas can be -30~-70 degrees Celsius.
According to an embodiment of the invention, the composition of the first liquid state cryogen is not particularly restricted, those skilled in the art
It can make choice according to actual needs, according to a particular embodiment of the invention, the first liquid state cryogen can contain 5~10%
The nitrogen of parts by volume；The methane of 20~30% parts by volume；The ethylene of 25~35% parts by volume；The propane of 10~20% parts by volume；
And 10~20% parts by volume isopentane., inventor has found, appropriate to increase heavy constituent content, such as isopentane in cryogen composition,
Be conducive to improve efficiency of heat exchanger and reduce the power of compressor, but content excessively easily causes the liquid at suction port of compressor again
Phenomenon is hit, and suitably increases light component content, such as nitrogen, can reduce refrigerant global cycle amount, so as to reduce compressor compresses
Work(, but when being to continue with increasing light component content, compressing the power consumption needed for specific discharge refrigerant increases, and causes total compression work(
Increase, and light component content excessively can cause heat exchanger before and after Load Distribution it is unreasonable, therefore, in azeotrope, nothing
By being heavy constituent or light component, only accomplish the reasonable distribution between component, system can just be made to reach best operation effect
Fruit and minimum operation energy consumption.
According to an embodiment of the invention, stage compressor 500 has the 3rd gaseous state cryogen import 501 and one stage of compression cryogen
Outlet 502, the 3rd gaseous state cryogen import 501 are connected with the first gaseous state cryogen outlet 205, and suitable for the first gaseous state cryogen is carried out
One stage of compression processing, so as to obtain one stage of compression cryogen.Gaseous state cryogen can be changed by gas by one stage of compression as a result,
The one stage of compression cryogen of liquid mixing.
According to an embodiment of the invention, the pressure of one stage of compression cryogen is not particularly restricted, and those skilled in the art can
To make choice according to actual needs, according to a particular embodiment of the invention, the pressure of one stage of compression cryogen can be 1.0~
2.0MPa(A).Inventor has found, if hypotony, split-compressor entrance tolerance increases, and energy consumption is caused to increase, is thus being pressed
In the range of contracting machine pressure ratio, stage compressor outlet pressure is improved as far as possible, so as to reduce total compression work(.
According to an embodiment of the invention, there is level-one cooler 600 one stage of compression cryogen import 601 and azeotrope to export
602, one stage of compression cryogen import 601 is connected with one stage of compression cryogen outlet 502, and suitable for one stage of compression cryogen is carried out level-one
Cooling treatment, so as to obtain azeotrope.It should be noted that those skilled in the art can be according to actual needs to this
The condition of level-one cooling treatment makes choice, such as level-one cooling treatment can carry out at 35~40 DEG C.
According to an embodiment of the invention, there is knockout drum 700 azeotrope import 701, the 4th gaseous state cryogen to export
702 and the 4th liquid refrigerant outlet 703, azeotrope import 701 and azeotrope outlet 602 is connected, and is suitable for mix cold
Agent carries out separating treatment, so as to obtain the 4th gaseous state cryogen and the 4th liquid refrigerant.
According to an embodiment of the invention, split-compressor 800 has the 4th gaseous state cryogen import 801 and two-stage compression cryogen
Outlet 802, the 4th gaseous state cryogen import 801 are connected with the 4th cryogen outlet 702, and suitable for the 4th gaseous state cryogen is carried out two level
Compression is handled, so as to obtain two-stage compression cryogen.It as a result, can be cold by the 4th isolated gaseous state by two-stage compression
Agent boil down to high-pressure gaseous cryogen.
According to an embodiment of the invention, the pressure of two-stage compression cryogen is not particularly restricted, and those skilled in the art can
To make choice according to actual needs, according to a particular embodiment of the invention, the pressure of two-stage compression cryogen can be 2.5~
5.0MPa(A).Inventor has found that influence of the split-compressor outlet pressure for system energy consumption is the knot of many-sided comprehensive function
Fruit, raised trend after the presentation of system total energy consumption is first reduced as outlet pressure reduces, research find the component according to cryogen
Difference, select 2.5~5.0MPa (A) outlet pressure it is the most economical.
According to an embodiment of the invention, secondary coolers 900 are cold with the import 901 of two-stage compression cryogen and the 5th liquid state
Agent outlet 902, two-stage compression cryogen import 901 and two-stage compression cryogen outlet 802 are connected, and be suitable for by two-stage compression cryogen into
Row two level cooling treatment, so as to obtain the 5th liquid state cryogen.It should be noted that those skilled in the art can basis
Actual needs makes choice the condition of the two level cooling treatment, such as secondary coolers outlet temperature can be controlled 35~40
It is carried out at DEG C.
According to an embodiment of the invention, distributor 1000 has the 4th liquid refrigerant import 1001, the 5th liquid state cryogen
Import 1002, liquid refrigerant outlet 1003 and gaseous state cryogen outlet 1004, the 4th liquid refrigerant import 1001 and the 4th liquid are cold
Agent outlet 703 is connected, and the 5th liquid state cryogen import 1002 is connected with the 5th liquid state cryogen outlet 902, liquid refrigerant outlet
1003 and the outlet of gaseous state cryogen 1004 be connected respectively with the first liquid state cryogen import 203, and suitable for by the 4th liquid refrigerant with
Gas-liquid separation is handled after 5th liquid state cryogen is mixed, so as to obtain liquid refrigerant and gaseous state cryogen, and by gained
Liquid refrigerant and gaseous state cryogen are respectively fed to heat exchanger and are used as the first liquid state cryogen.
Liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention passes through in the different positions of heat exchanger
It puts and two methane gas imports is set, and on the methane gas conveying pipe between methane gas storage tank and methane gas import respectively
Control valve is set, it can be according to the feeding temperature adjusting control valve of methane gas, so as to the methane gas stream to two methane gas imports
Amount is adjusted so that the evaporation curve of cryogen and the cooling liquid curve of methane gas be most in heat exchanger at a temperature of different methane gas
The matching of limits, and then can realize the maximization of heat exchanger heat exchange efficiency, and then the liquefaction efficiency of methane gas is improved, and
Have the advantages that low energy consumption, variable working condition ability is strong, technological process is simple and investment is low, while singly followed using the throttling of cryogen single
The technique of ring, short flow in ice chest, number of devices is few, characteristics of compact layout, compared with traditional multistage cooling liquid flow, reduces cold
Cryo Equipment, instrument and pipeline in case reduce ice chest size, 30% investment, and refrigeration cycle are at least saved than traditional handicraft
Compression power consumption is relatively low, and main heat exchanger and ice chest size are small, is conducive to the production domesticization of key equipment and the enlargement of liquefying plant.
With reference to figure 3, the liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention further comprises delaying
Rush tank 1100 and liquid phase pump 1200.
According to an embodiment of the invention, surge tank 1100 respectively with the first gaseous state cryogen outlet 205 and the 3rd gaseous state cryogen
Import 501 is connected, and suitable for being supplied by the obtained in heat exchanger first gaseous state cryogen to stage compressor progress one stage of compression
Before, the first gaseous state cryogen is supplied into surge tank in advance.Thus, it is possible to significantly improve the operation stability of liquefaction system.
According to an embodiment of the invention, liquid phase pump 1200 respectively with the 4th liquid refrigerant outlet 703 and the 4th liquid refrigerant
Import 1001 is connected, and is driven into suitable for will obtain the 4th liquid refrigerant in knockout drum 700 in distributor 1000.
It is selected from as described above, the liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention can have
At least one the advantages of following：
Liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention can be directed to the first of different temperatures
Alkane gas feed state, by flow-rate adjustment, the feed inlet position that selects heat exchanger different, make methane gas cooling liquid curve with
Azeotrope evaporation curve coincide to greatest extent, improves heat exchanger efficiency；
Cryogen level-one suitable for the liquefaction system of different temperatures methane gas throttling flow according to embodiments of the present invention
More stages throttling saves Cryo Equipment, instrument and the pipeline in ice chest, 30% throwing is at least saved than traditional handicraft compared to simply
Money, and power consumption is relatively low；
Liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention shares heat using two heat exchangers
Load is conducive to the production domesticization and enlargement of key equipment；
Liquefaction system suitable for different temperatures methane gas according to embodiments of the present invention makes full use of methane gas liquefaction to fill
The existing technique and equipment of front end are put, carries out the precooling of methane gas, methane gas liquefying plant is avoided and newly goes up pre- cold flow and set
It is standby, energy consumption is reduced, reduces investment.
In another aspect of the invention, the present invention proposes a kind of method of liquefied methane gas.Reality according to the present invention
Example is applied, this method is so that being carried out suitable for the liquefaction system of different temperatures methane gas using described above.According to the present invention
Specific embodiment, this method includes：Methane gas is supplied, heat exchange processing is carried out into the heat exchanger, so that the first
Alkane gas and the first liquid state cryogen carry out heat exchange processing, to obtain the first gaseous state cryogen and liquefied methane gas；By described first
Gaseous state cryogen, which is supplied into the stage compressor, carries out one stage of compression processing, to obtain one stage of compression cryogen；By described one
Grade compression cryogen, which is supplied into the level-one cooler, carries out level-one cooling treatment, to obtain azeotrope；By the mixing
Cryogen, which is supplied, carries out separating treatment into the knockout drum, to obtain the 4th gaseous state cryogen and the 4th liquid refrigerant；It will
The 4th gaseous state cryogen, which is supplied into the split-compressor, carries out two-stage compression processing, to obtain two-stage compression cryogen；
The two-stage compression cryogen is supplied into the secondary coolers and carries out two level cooling treatment, it is cold to obtain the 5th liquid state
Agent；4th liquid refrigerant and the 5th liquid state cryogen are supplied into the distributor and mix laggard promoting the circulation of qi liquid point
From to obtain liquid refrigerant and gaseous state cryogen, and the gaseous state cryogen and the liquid refrigerant being respectively fed to described change
Hot device is used as the first liquid state cryogen.Inventor has found, by using the above-mentioned liquefaction suitable for different temperatures methane gas
System can realize that the evaporation curve of cryogen and the cooling liquid curve of methane gas are maximum in heat exchanger at a temperature of different methane gas
The matching of limit so as to realize the maximization of heat exchanger heat exchange efficiency, and then improves the liquefaction efficiency of methane gas, and has
Have that low energy consumption, variable working condition ability is strong, technological process is simple and the low advantage of investment.It is it should be noted that above-mentioned for applicable
In the method that the described feature and advantage of the liquefaction system of different temperatures methane gas are equally applicable to the liquefied methane gas, herein
It repeats no more.
It is described in detail below with reference to the method for the liquefied methane gas of Fig. 4-5 pairs of embodiment of the present invention.According to the present invention
Embodiment, this method includes：
S100：Methane gas is supplied into heat exchanger and carries out heat exchange processing
According to an embodiment of the invention, methane gas is supplied into heat exchanger and carries out heat exchange processing so that methane gas and the
One liquid state cryogen carries out heat exchange processing, so as to obtain the first gaseous state cryogen and liquefied methane gas.
According to a particular embodiment of the invention, step S100 is carried out according to the following steps：
S110：First liquid state cryogen is supplied to first cold heat exchanger
According to an embodiment of the invention, the first liquid state cryogen is supplied to first cold heat exchanger, so as to obtain just gas
Liquid refrigerant.A specific embodiment according to the present invention, the temperature of first liquid state cryogen can be -30~-70 degrees Celsius.
S120：First liquid state cryogen is supplied to whole cold heat exchanger
According to an embodiment of the invention, the first liquid state cryogen first cold heat exchanger obtained is supplied to whole cold heat exchanger, from
And the second liquid refrigerant can be obtained.Another specific embodiment according to the present invention, the temperature of the second liquid refrigerant can be-
140~-165 degrees Celsius.
S130：Second liquid refrigerant is supplied to throttle valve
According to an embodiment of the invention, the second liquid refrigerant is supplied to throttle valve, it is cold so as to obtain whole liquid state
Agent.A specific embodiment according to the present invention, the temperature of whole liquid state cryogen can be -145~-170 degrees Celsius, and pressure can
Think 0.2~0.5MPa (A).
S140：The part supply of methane gas to whole cold heat exchanger and whole liquid state cryogen is exchanged heat
According to an embodiment of the invention, the part supply of methane gas to whole cold heat exchanger and whole liquid state cryogen are carried out
Heat exchange, so as to cryogen and liquefied methane gas after being exchanged heat.
S150：Another part of methane gas is supplied and is exchanged heat into first cold heat exchanger with cryogen after heat exchange, and will be just
Supply exchanges heat into whole cold heat exchanger with whole liquid state cryogen after cold methane gas is mixed with a part for methane gas
According to an embodiment of the invention, by another part of methane gas supply into first cold heat exchanger with cryogen after heat exchange into
Row heat exchange, so as to obtain just cold methane gas and the first gaseous state cryogen, and by one of first cold methane gas and methane gas
Divide after mixing to supply and exchange heat into whole cold heat exchanger with whole liquid state cryogen.A specific embodiment according to the present invention,
The temperature of first cold methane gas can be -30~-70 degrees Celsius.
A specific embodiment according to the present invention is made just cold by the aperture for adjusting the first control valve, the second control valve
The mixing temperature of a part for methane gas and methane gas, when mixing temperature is less than -70 degrees Celsius, turns the down at -30~-70 DEG C
One control valve tunes up the second control valve so that most of methane gas is supplied to whole cold heat exchanger, and fraction methane gas is supplied to first
Cold heat exchanger,
The temperature of another specific embodiment according to the present invention, first cold methane gas and the second methane gas is Celsius higher than -30
Degree, tunes up the first control valve, turns the second control valve down so that most of methane gas is supplied to first cold heat exchanger, fraction methane
Gas is supplied to whole cold heat exchanger.As a result, by using the first cold heat exchanger that is connected with each other and whole cold heat exchanger, and by the first methane
Gas import and the second methane gas import are separately positioned on just cold heat exchanger and whole cold heat exchanger, are conveyed by being arranged on methane gas
The first control valve and the second control valve on pipeline, can be according to the feeding temperature adjusting control valve of methane gas, respectively to entering
The methane gas flow of first cold heat exchanger and whole cold heat exchanger is adjusted so that cryogen in heat exchanger at a temperature of different methane gas
Evaporation curve matches to greatest extent with the cooling liquid curve of methane gas, and then can realize the maximum of heat exchanger heat exchange efficiency
Change, and then improve the liquefaction efficiency of methane gas, and with low energy consumption, variable working condition ability is strong, technological process is simple and investment
Low advantage.
S200：First gaseous state cryogen is supplied into stage compressor and carries out one stage of compression processing
According to an embodiment of the invention, obtained first gaseous state cryogen is supplied into stage compressor and carries out level-one pressure
Contracting is handled, so as to obtain one stage of compression cryogen.Gaseous state cryogen can be changed into the one of gas-liquid mixed by one stage of compression as a result,
Grade compression cryogen.
According to an embodiment of the invention, the pressure of one stage of compression cryogen is not particularly restricted, and those skilled in the art can
To make choice according to actual needs, according to a particular embodiment of the invention, the pressure of one stage of compression cryogen can be 1.0~
2.0MPa(A).Inventor has found, if hypotony, split-compressor entrance tolerance will increase, and energy consumption is caused to increase, is thus existed
In the range of the pressure ratio of stage compressor, stage compressor outlet pressure is improved as far as possible, it is favourable to reducing total compression work(and energy consumption.
S300：One stage of compression cryogen is supplied into level-one cooler and carries out level-one cooling treatment
According to one embodiment of present invention, one stage of compression cryogen is supplied into level-one cooler and carried out at level-one cooling
Reason, so as to obtain azeotrope.It should be noted that those skilled in the art can be cold to the level-one according to actual needs
But the condition handled makes choice, and level-one cooler outlet temperature can be controlled at 30~40 DEG C.
S400：Azeotrope is supplied into knockout drum and carries out separating treatment
According to an embodiment of the invention, azeotrope is supplied into knockout drum and carries out separating treatment, so as to
Obtain the 4th gaseous state cryogen and the 4th liquid refrigerant.
S500：4th gaseous state cryogen is supplied into split-compressor and carries out two-stage compression processing
According to an embodiment of the invention, the 4th gaseous state cryogen is supplied into split-compressor and carries out two-stage compression processing,
So as to obtain two-stage compression cryogen.It as a result, can be by the 4th isolated gaseous state cryogen boil down to by two-stage compression
Liquid refrigerant.
According to an embodiment of the invention, the pressure of two-stage compression cryogen is not particularly restricted, and those skilled in the art can
To make choice according to actual needs, according to a particular embodiment of the invention, the pressure of two-stage compression cryogen can be 2.5~
5.0MPa(A).Inventor has found that influence of the split-compressor outlet pressure for system energy consumption is the knot of many-sided comprehensive function
Fruit, raised trend after the presentation of system total energy consumption is first reduced as outlet pressure reduces, research find the component according to cryogen
Difference, select 2.5~5.0MPa (A) the most economical.
S600：Two-stage compression cryogen is supplied into secondary coolers and carries out two level cooling treatment
According to an embodiment of the invention, two-stage compression cryogen is supplied into secondary coolers and carries out two level cooling treatment,
So as to obtain the 5th liquid state cryogen.It should be noted that those skilled in the art can according to actual needs to this two
The condition of grade cooling treatment makes choice, and secondary coolers outlet temperature can be controlled at 30~40 DEG C.
S700：It is carried out after 4th liquid refrigerant and the 5th liquid state cryogen are supplied into distributor mixing at gas-liquid separation
Reason, and liquid refrigerant and gaseous state cryogen are supplied to heat exchanger as the first liquid state cryogen
According to an embodiment of the invention, after the 4th liquid refrigerant and the 5th liquid state cryogen being supplied into distributor mixing
Gas-liquid separation is carried out, so as to obtain liquid refrigerant and gaseous state cryogen, and liquid refrigerant and gaseous state cryogen are supplied to heat exchange
Device is used as the first liquid state cryogen.
The method of liquefied methane gas according to embodiments of the present invention is by using above-mentioned suitable for different temperatures methane gas
Liquefaction system can realize at a temperature of different methane gas the evaporation curve of cryogen and the cooling liquid curve of methane gas in heat exchanger
It matches to greatest extent, so as to realize the maximization of heat exchanger heat exchange efficiency, and then improves the liquefaction efficiency of methane gas, and
And have the advantages that low energy consumption, variable working condition ability is strong, technological process is simple and investment is low.
According to an embodiment of the invention, the first gaseous state cryogen is being supplied into stage compressor progress one stage of compression processing
Before, the first gaseous state cryogen is supplied into surge tank in advance.Thus, it is possible to significantly improve the operation stability of liquefaction system.
According to an embodiment of the invention, liquid phase pump may be employed and be driven into the 4th liquid refrigerant is obtained in knockout drum
In distributor.
Below with reference to specific embodiment, present invention is described, it is necessary to which explanation, these embodiments are only to describe
Property, without limiting the invention in any way.
Embodiment
Methane gas is handled using the liquefaction system suitable for different temperatures methane gas of Fig. 1~3 of the present invention,
In, the composition of cryogen is：The nitrogen of 6V%, the methane of 27.6V%, the ethylene of 31.3V%, 17.5V% propane and
The isopentane of 17.6V%, the composition of methane gas are：The methane of 96.4V%, the ethane of 1.5V%, 1.3V% carbon monoxide,
The hydrogen of 0.3V% and the nitrogen of 0.5V%, the temperature of methane gas is -20 DEG C, the first control valve opening 30~40%, second
Control valve opening 50~60%, the temperature of first liquid state cryogen is -30~-70 degrees Celsius, the temperature of the second liquid refrigerant for -
140~-170 degrees Celsius, the temperature of whole liquid refrigerant is -135~-190 degrees Celsius, and pressure is 0.2~0.5MPa (A), just cold
The temperature of methane gas is -25~-45 degrees Celsius, and the pressure of one stage of compression cryogen is 1.0~2.0MPa (A), two-stage compression cryogen
Pressure be 2.5~5.0MPa (A).The composition of obtained liquefied methane gas is the methane of 96.7V%, the ethane of 1.8V%,
The carbon monoxide of 1.1V% and the hydrogen of 0.4V%.
In the description of this specification, reference term " one embodiment ", " some embodiments ", " example ", " specifically show
The description of example " or " some examples " etc. means specific features, structure, material or the spy for combining the embodiment or example description
Point is contained at least one embodiment of the present invention or example.In the present specification, schematic expression of the above terms is not
It must be directed to identical embodiment or example.Moreover, particular features, structures, materials, or characteristics described can be in office
It is combined in an appropriate manner in one or more embodiments or example.In addition, without conflicting with each other, the skill of this field
Art personnel can tie the different embodiments described in this specification or example and different embodiments or exemplary feature
It closes and combines.
Although the embodiment of the present invention has been shown and described above, it is to be understood that above-described embodiment is example
Property, it is impossible to limitation of the present invention is interpreted as, those of ordinary skill in the art within the scope of the invention can be to above-mentioned
Embodiment is changed, changes, replacing and modification.
Claims (15)
1. a kind of liquefaction system suitable for different temperatures methane gas, which is characterized in that including：
Methane gas storage tank；
Heat exchanger, the heat exchanger have the first methane gas import, the second methane gas import, the first liquid state cryogen import, the
Two liquid state cryogen imports, the outlet of the first gaseous state cryogen, the outlet of the second liquid refrigerant and liquefied methane gas outlet, first first
The import of alkane gas, the first liquid state cryogen import and the first gaseous state cryogen outlet are arranged on the front end of the heat exchanger,
The second methane gas import is arranged in the middle part of the heat exchanger, the second liquid state cryogen import and second liquid are cold
Agent, which exports, is arranged on the end of the heat exchanger, the first methane gas import and the second methane gas import respectively with it is described
Methane gas storage tank is connected, and in the methane gas storage tank and the first methane gas import and the second methane gas import
The first control valve and the second control valve are respectively arranged on methane gas conveying pipe, the second liquid state cryogen import passes through cold
Agent pipeline is connected with second liquid refrigerant outlet, and throttle valve is provided on the cryogen pipeline；
Liquefied pot, the liquefied pot are connected with liquefied methane gas outlet；
There is the 3rd gaseous state cryogen import and one stage of compression cryogen to export for stage compressor, the stage compressor, and the described 3rd
The import of gaseous state cryogen is connected with the first gaseous state cryogen outlet；
There is the import of one stage of compression cryogen and azeotrope to export for level-one cooler, the level-one cooler, the one stage of compression
Cryogen import is connected with one stage of compression cryogen outlet；
Knockout drum, the knockout drum have azeotrope import, the outlet of the 4th gaseous state cryogen and the 4th liquid refrigerant
Outlet, the azeotrope import are connected with azeotrope outlet；
There is the 4th gaseous state cryogen import and two-stage compression cryogen to export for split-compressor, the split-compressor, and the described 4th
The import of gaseous state cryogen is connected with the 4th gaseous state cryogen outlet；
There is the import of two-stage compression cryogen and the 5th liquid state cryogen to export for secondary coolers, the secondary coolers, and described two
Grade compression cryogen import is connected with two-stage compression cryogen outlet；
Distributor, the distributor are gentle with the 4th liquid refrigerant import, the 5th liquid state cryogen import, liquid refrigerant outlet
State cryogen exports, and the 4th liquid refrigerant import is connected with the 4th liquid refrigerant outlet, the 5th liquid state cryogen
The outlet of import and the 5th liquid state cryogen is connected, the gaseous state cryogen outlet and the liquid refrigerant export respectively with it is described
First liquid state cryogen import is connected；
Surge tank, the surge tank are connected respectively with the first gaseous state cryogen outlet and the 3rd gaseous state cryogen import；
Liquid phase pump, the liquid phase pump are connected respectively with the 4th liquid refrigerant outlet and the 4th liquid refrigerant import,
Wherein, the heat exchanger includes first cold heat exchanger and whole cold heat exchanger, the just cold heat exchanger have after heat exchange cryogen into
Mouth, the outlet of first liquid state cryogen and just cold methane gas outlet, after the end cold heat exchanger is with first liquid state cryogen import, heat exchange
Cryogen exports and first cold methane gas import, after the heat exchange cryogen import be connected with cryogen outlet after the heat exchange, the first gas
Liquid refrigerant is exported to be connected with the just liquid state cryogen import, the just cold methane gas outlet and the second methane gas import
Respectively with it is described just cold methane gas import be connected, and the first methane gas import, the first liquid state cryogen import and
The first gaseous state cryogen outlet is arranged on the just cold heat exchanger, the second liquid state cryogen import and second liquid
The outlet of state cryogen is arranged on the whole cold heat exchanger.
2. system according to claim 1, which is characterized in that by adjusting first control valve and second control
The aperture of valve, the mixing temperature for controlling just cold methane gas and the second methane gas is -30~-70 degrees Celsius.
3. system according to claim 2, which is characterized in that when the mixing temperature is less than -70 degrees Celsius, turn institute down
The first control valve is stated, tunes up second control valve.
4. system according to claim 3, which is characterized in that when the mixing temperature is higher than -30 degrees Celsius, tune up institute
The first control valve is stated, turns second control valve down.
The first 5. a kind of liquefaction system according to any one of claims 1 to 4 suitable for different temperatures methane gas liquefies
The method of alkane gas, which is characterized in that including：
Methane gas is supplied, heat exchange processing is carried out into the heat exchanger, so that the methane gas and the first liquid state cryogen
Heat exchange processing is carried out, to obtain the first gaseous state cryogen and liquefied methane gas；
The first gaseous state cryogen is supplied into the stage compressor and carries out one stage of compression processing, to obtain one stage of compression
Cryogen；
The one stage of compression cryogen is supplied into the level-one cooler and carries out level-one cooling treatment, it is cold to obtain mixing
Agent；
The azeotrope is supplied, separating treatment is carried out into the knockout drum, to obtain the 4th gaseous state cryogen and
Four liquid refrigerants；
The 4th gaseous state cryogen is supplied into the split-compressor and carries out two-stage compression processing, to obtain two-stage compression
Cryogen；
The two-stage compression cryogen is supplied into the secondary coolers and carries out two level cooling treatment, to obtain the 5th gas-liquid
State cryogen；
4th liquid refrigerant and the 5th liquid state cryogen are supplied into the distributor and mix laggard promoting the circulation of qi liquid point
From to obtain liquid refrigerant and gaseous state cryogen, and the gaseous state cryogen and the liquid refrigerant being respectively fed to described change
Hot device is used as the first liquid state cryogen.
6. according to the method described in claim 5, it is characterized in that, heat exchange processing is carried out according to the following steps：
The first liquid state cryogen is supplied to the just cold heat exchanger, to obtain just liquid state cryogen；
The just liquid state cryogen is supplied to the whole cold heat exchanger, to obtain the second liquid refrigerant；
Second liquid refrigerant is supplied to the throttle valve, to obtain whole liquid state cryogen；
The part supply of the methane gas to the whole cold heat exchanger and the whole liquid state cryogen is exchanged heat, so as to
Cryogen and liquefied methane gas after to heat exchange；
Another part of the methane gas is supplied and is exchanged heat into the just cold heat exchanger with cryogen after the heat exchange, so as to
Obtain just cold methane gas and the first gaseous state cryogen, and will the just cold methane gas and the methane gas it is a part of mix after
Supply exchanges heat into the whole cold heat exchanger with the whole liquid state cryogen.
7. according to the method described in claim 6, it is characterized in that, by adjusting first control valve and second control
The aperture of valve, the mixing temperature for controlling the just cold methane gas and a part for the methane gas is -30~-70 degrees Celsius.
8. the method according to the description of claim 7 is characterized in that when the mixing temperature is less than -70 degrees Celsius, institute is turned down
The first control valve is stated, tunes up second control valve, so that most of methane gas is supplied to the whole cold heat exchanger, small portion
Point methane gas is supplied to the just cold heat exchanger.
9. the method according to the description of claim 7 is characterized in that when the mixing temperature is higher than -30 degrees Celsius, institute is tuned up
The first control valve is stated, turns second control valve down, so that most of methane gas is supplied to the just cold heat exchanger, small portion
Point methane gas is supplied to the whole cold heat exchanger.
10. according to the method described in claim 6, it is characterized in that, the temperature of the just liquid state cryogen is taken the photograph for -30~-70
Family name's degree.
11. according to the method described in claim 6, it is characterized in that, the temperature of second liquid refrigerant is -140~-165
Degree Celsius.
12. according to the method described in claim 6, it is characterized in that, the temperature of the end liquid state cryogen is -145~-170
Degree Celsius, pressure is 0.2~0.5MPa (A).
13. the method according to claim 6 or 7, which is characterized in that the temperature of the just cold methane gas is taken the photograph for -30~-70
Family name's degree.
14. according to the method described in claim 5, it is characterized in that, the pressure of the two-stage compression cryogen is 2.5~5.0MPa
(A)。
15. according to the method described in claim 5, it is characterized in that, the first liquid state cryogen contains：
The nitrogen of 5~10% parts by volume；
The methane of 20~30% parts by volume；
The ethylene of 25~35% parts by volume；
The propane of 10~20% parts by volume；And
The isopentane of 10~20% parts by volume.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610105153.1A CN105651001B (en) | 2016-02-25 | 2016-02-25 | Liquefaction system suitable for different temperatures methane gas and the method using the system liquefied methane gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610105153.1A CN105651001B (en) | 2016-02-25 | 2016-02-25 | Liquefaction system suitable for different temperatures methane gas and the method using the system liquefied methane gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105651001A CN105651001A (en) | 2016-06-08 |
| CN105651001B true CN105651001B (en) | 2018-05-22 |
Family
ID=56488817
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610105153.1A Active CN105651001B (en) | 2016-02-25 | 2016-02-25 | Liquefaction system suitable for different temperatures methane gas and the method using the system liquefied methane gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105651001B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP6741565B2 (en) * | 2016-12-08 | 2020-08-19 | 川崎重工業株式会社 | Raw material gas liquefier and control method thereof |
| CN111947240B (en) * | 2020-08-10 | 2021-12-31 | 浙江申永达设备安装有限公司 | Special refrigerating machine room module for rail transit |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3914949A (en) * | 1971-02-19 | 1975-10-28 | Chicago Bridge & Iron Co | Method and apparatus for liquefying gases |
| US4586942A (en) * | 1983-02-08 | 1986-05-06 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas |
| CN1451090A (en) * | 2000-06-09 | 2003-10-22 | 布拉克及维特奇普里特查德有限公司 | Improved closed loop single mixed refrigerant process |
| CN101413749A (en) * | 2008-11-20 | 2009-04-22 | 成都赛普瑞兴科技有限公司 | Method and apparatus for single-stage mixing cryogen refrigerating cycle liquefied natural gas |
| CN101608860A (en) * | 2008-06-17 | 2009-12-23 | 北京安瑞科新能能源科技有限公司 | Gas liquefying process for mixed refrigerant and mix refrigerant |
| KR20110076214A (en) * | 2009-12-29 | 2011-07-06 | 지에스건설 주식회사 | Liquefaction of natural gas |
| CN205482103U (en) * | 2016-02-25 | 2016-08-17 | 上海尧兴投资管理有限公司 | Liquefaction system suitable for different temperatures methane gas |
-
2016
- 2016-02-25 CN CN201610105153.1A patent/CN105651001B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3914949A (en) * | 1971-02-19 | 1975-10-28 | Chicago Bridge & Iron Co | Method and apparatus for liquefying gases |
| US4586942A (en) * | 1983-02-08 | 1986-05-06 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and plant for the cooling of a fluid and in particular the liquefaction of natural gas |
| CN1451090A (en) * | 2000-06-09 | 2003-10-22 | 布拉克及维特奇普里特查德有限公司 | Improved closed loop single mixed refrigerant process |
| CN101608860A (en) * | 2008-06-17 | 2009-12-23 | 北京安瑞科新能能源科技有限公司 | Gas liquefying process for mixed refrigerant and mix refrigerant |
| CN101413749A (en) * | 2008-11-20 | 2009-04-22 | 成都赛普瑞兴科技有限公司 | Method and apparatus for single-stage mixing cryogen refrigerating cycle liquefied natural gas |
| KR20110076214A (en) * | 2009-12-29 | 2011-07-06 | 지에스건설 주식회사 | Liquefaction of natural gas |
| CN205482103U (en) * | 2016-02-25 | 2016-08-17 | 上海尧兴投资管理有限公司 | Liquefaction system suitable for different temperatures methane gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105651001A (en) | 2016-06-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US6295833B1 (en) | Closed loop single mixed refrigerant process | |
| US8650906B2 (en) | System and method for recovering and liquefying boil-off gas | |
| CN101893367B (en) | Method for liquefying natural gas by using mixed coolant | |
| CA2856096C (en) | System and method for liquefying natural gas using single mixed refrigerant as refrigeration medium | |
| US20150013378A1 (en) | Apparatus And Method For Liquefying Natural Gas By Refrigerating Single Mixed Working Medium | |
| CN103857955A (en) | Pressure rise suppression device for storage tank, pressure rise suppression system provided therewith, suppression method therefor, liquefied gas carrying vessel provided therewith, and liquefied gas storage facility provided therewith | |
| AU2001264058A1 (en) | Improved closed loop single mixed refrigerant process | |
| CN101392983B (en) | Process for liquefying high methane gas | |
| JP2014142161A (en) | Manufacturing apparatus and method of low temperature compression gas or liquid gas | |
| CN206695421U (en) | LNG cold energy refrigerating circulatory devices | |
| CN102564059A (en) | Twin-stage multi-component mixed refrigerant refrigeration natural gas liquefaction system and method | |
| CN104807287A (en) | Small natural gas liquefaction and refrigeration system and small natural gas liquefaction and refrigeration method | |
| CN103038587A (en) | Natural Gas Liquefaction Process | |
| CN105651001B (en) | Liquefaction system suitable for different temperatures methane gas and the method using the system liquefied methane gas | |
| CN201532077U (en) | Natural gas liquefying device based on low temperature liquid refrigeration | |
| CN103216998A (en) | Method and system for compressing and conveying single-cycle mixed refrigerant | |
| CN101709912B (en) | Natural gas liquefying device based on low-temperature liquid refrigeration | |
| CN106595220B (en) | Liquefaction system for liquefying natural gas and liquefaction method thereof | |
| CN204630250U (en) | A kind of mini gas liquefying refrigerating system | |
| CN203349591U (en) | Device for making ice by utilizing cold energy of LNG (liquefied natural gas) satellite station | |
| CN102620460B (en) | Hybrid refrigeration cycle system and method with propylene pre-cooling | |
| KR101325586B1 (en) | Natural gas liquefaction system | |
| CN205482103U (en) | Liquefaction system suitable for different temperatures methane gas | |
| CN104457137B (en) | System and method for liquefying natural gas through multi-component refrigerant cycle refrigeration | |
| CN205593289U (en) | Liquefied natural gas's device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |