CN103017480A - Liquefaction system for producing LNG (Liquefied Natural Gas) by using pressure energy of pipeline - Google Patents
Liquefaction system for producing LNG (Liquefied Natural Gas) by using pressure energy of pipeline Download PDFInfo
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- CN103017480A CN103017480A CN2012105266479A CN201210526647A CN103017480A CN 103017480 A CN103017480 A CN 103017480A CN 2012105266479 A CN2012105266479 A CN 2012105266479A CN 201210526647 A CN201210526647 A CN 201210526647A CN 103017480 A CN103017480 A CN 103017480A
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- heat exchanger
- pipeline
- recuperative heat
- pressure
- branch road
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- 239000003949 liquefied natural gas Substances 0.000 title abstract description 39
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 96
- 239000003345 natural gas Substances 0.000 claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 44
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000001816 cooling Methods 0.000 claims abstract description 11
- 108091006146 Channels Proteins 0.000 claims description 72
- 238000000746 purification Methods 0.000 claims description 23
- 206010000060 Abdominal distension Diseases 0.000 claims description 21
- 208000024330 bloating Diseases 0.000 claims description 21
- 230000006835 compression Effects 0.000 claims description 12
- 238000007906 compression Methods 0.000 claims description 12
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000007791 liquid phase Substances 0.000 abstract 1
- 239000012071 phase Substances 0.000 abstract 1
- 230000006837 decompression Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000032258 transport Effects 0.000 description 3
- 239000002253 acid Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
- F25J1/0037—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work of a return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
- F25J1/0232—Coupling of the liquefaction unit to other units or processes, so-called integrated processes integration within a pressure letdown station of a high pressure pipeline system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
- F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
Abstract
The invention relates to a gas liquefaction system, and particularly relates to a liquefaction system for producing LNG (Liquefied Natural Gas) by using pressure energy of a pipeline. Natural gas from a high-pressure pipe is divided into natural gas in a liquefaction branch, natural gas in a first pre-cooling branch and natural gas in a main cooling branch, wherein the natural gas in the liquefaction branch is from the high-pressure pipeline, is sequentially compressed and cooled, then obtains heat in a backheating heat exchanger, and enters a gas-liquid separator after being throttled; a separated liquid phase is produced LNG; a gas phase enters a low-pressure pipeline after the cold energy is recycled by the backheating heat exchanger; the natural gas in the first pre-cooling branch enters the low-pressure pipeline after being expanded by an expanding machine after the cold energy is recycled in a heat regenerator; and the natural gas in the main cooling branch and the natural gas in the liquefaction branch are separated behind a cooler, the natural gas in the main cooling branch is cooled by the backheating heat exchanger and then throttled and expanded, and finally enters the low-pressure pipeline after the cold energy is recycled by the backheating heat exchanger. According to the liquefaction system, the LNG can be produced by using the pressure of the pipelines, compressors are driven by output works of the expanding machine without additional energy consumption.
Description
Technical field
The present invention relates to the liquefaction system of the LNG in derived energy chemical field, particularly a kind of liquefaction system that utilizes pipeline pressure can produce LNG.
Background technology
Natural gas is a kind of high-quality, efficient clean energy resource and industrial chemicals, is widely used in the every field of the development of the national economy.The natural gas pool of China nearly ninety percent concentrates on central and west regions, mainly transports to the east by gas line network, and annual design transport gas ability is at 90,000,000,000 m at present
3-1,000 hundred million m
3The natural gas trunk line is according to the difference of design; discharge pressure 4 to 10MPa; usually can be decompressed to the following recycling of 0.5～1.2MPa through the multi-step pressure reduction station after being transported to the destination; this decompression process is taked direct throttling usually; the a large amount of pressure energy that wherein discharges is not utilized; even avoid cold that throttling produces that pipeline and equipment are caused damage and need gas after the additive decrementation energy heats throttling, cause serious high-grade energy waste.On the other hand, because low-pressure pipe network laying limitation, being limited in scope of the rear supply of high pressure pipe network decompression still has a large amount of pipe networks user in addition can't utilize natural gas resource, needs in addition purchase compressed natural gas or liquefied natural gas.Therefore, utilize the pressure differential between the high-low pressure pipeline in the gas distributing system, the process realizing a large amount of high-pressure natural gas decompressions with wherein part natural gas liquefaction, obtains LNG, with the user beyond the supply pipe network, is a kind of solution of killing two birds with one stone.The several technical scheme of utilizing the pipeline pressure energy is arranged at present, and for example patent CN202393170 all mentions among CN202139209 and the CN1409812A.For the higher situation of low pressure pipeline pressure, the natural gas after the expansion needs to enter low pressure pipeline through overcompression again among its Patent CN202393170, and the work done during compression of flash gas needs extra the supply, and system needs extra power consumption.Expansion work among the patent CN202139209 is not utilized, and system needs extra power consumption.And among the patent CN1409812A, gas returns circulation after the expansion of precooling branch road after recompression, and still energy consumption is larger can to make like this raising of system liquid rate.In sum, the existing electrically-driven compressors that utilizes that utilizes pipeline pressure energy LNG Technology to have improves gas pressure, what have utilizes the precooling of electric-driven refrigerating machine, still needs the additional energy input in the situation that reach higher liquefied fraction, and the pressure energy utilization rate is not high.The present patent application proposes a kind of system and utilizes pipeline pressure can produce the technical scheme of LNG, obtain cold by the natural gas expansion from pressure duct, the pressure energy of natural gas is converted into cold energy, realize the liquefaction of part natural gas, produce the LNG product and can be used as commodity, also can be used for peak regulation.The portion gas that is used for precooling in the system need not to do deep purifying, has alleviated purification pressure.
Summary of the invention
The object of the invention is to propose a kind of gas liquefaction system that utilizes pipeline can produce LNG, this system can utilize the pressure differential between the high-low pressure pipeline in the Natural gas letdown station, with the part natural gas liquefaction, need not extra power consumption, when realizing the high-pressure air source decompression, production part LNG.
Technical scheme of the present invention is as follows:
The liquefaction system that utilizes pipeline pressure can produce LNG provided by the invention has two kinds of schemes.
Described the first liquefaction system that utilizes pipeline pressure can produce LNG provided by the invention, it comprises:
The first class purification device P1 that links to each other with the outlet of gas pipeline pressure piping, the first distributing valve T1 is installed on the described first class purification device P1 export pipeline, and described first class purification device P1 export pipeline is divided into first paragraph liquefaction branch road M01 and the first precooling branch road M1 two-way through this first distributing valve T1; Described first paragraph liquefaction branch road M01 is for being connected in successively the first compressor C1 and the first cooler D1 behind the first distributing valve T1;
Be connected in the second cleaner P2 on described the first cooler D1 export pipeline, the second distributing valve T2 is installed on the described second cleaner P2 export pipeline, described second cleaner P2 export pipeline divides two pipelines through this second distributing valve T2, and this two pipeline is second segment liquefaction branch road M02 and main cold branch road M2; Described second segment liquefaction branch road M02 is the high-pressure channel that is connected in successively the first Recuperative heat exchanger H1 behind the second distributing valve T2, high-pressure channel, first throttle bloating plant V1 and the gas-liquid separator S1 of the second Recuperative heat exchanger H2; The cold branch road M2 of described master is for being connected in successively high-pressure channel, the high-pressure channel of the second Recuperative heat exchanger H2, the low-pressure channel of the second throttling bloating plant V2, the second Recuperative heat exchanger H2, the low-pressure channel of the first Recuperative heat exchanger H2 and the low pressure pipeline of gas pipeline of the first Recuperative heat exchanger H1 behind the second distributing valve T2;
The outlet of described gas-liquid separator S1 bottom is the LNG product outlet, and the outlet of gas-liquid separator S1 top connects the low-pressure channel of the second Recuperative heat exchanger H2, the low-pressure channel of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively;
The first precooling branch road M1 is the first decompressor E1 that is connected in the first distributing valve T1, and this first decompressor E1 connects the low-pressure channel of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively; The work done during compression of described the first compressor C1 is from the expansion work of the first decompressor E1.
Described first throttle bloating plant V1 is choke valve.
The liquefaction system that utilizes pipeline pressure can produce LNG provided by the invention also can comprise the second compressor C2 and the second cooler D2, and described the second throttling bloating plant V2 is the second decompressor E2; Described the second compressor C2 and the second cooler D2 are connected in behind the second distributing valve T2 and between the pressure piping of described the first Recuperative heat exchanger H1 on the pipeline successively; The work done during compression of described the second compressor C2 is from the expansion work of the second decompressor E2.
Described the first cooler D1 and the second cooler D2 are water-cooling cooler or air-cooled cooler; The cooler outlet natural gas temperature is 10～40 ℃.
Described the second liquefaction system that utilizes pipeline pressure can produce LNG provided by the invention, it comprises:
The first class purification device P1 that links to each other with the outlet of gas pipeline pressure piping, the first distributing valve T1 is installed on the described first class purification device P1 export pipeline, and described first class purification device P1 export pipeline is divided into first paragraph liquefaction branch road M01 and the first precooling branch road M1 two-way through the first distributing valve T1; Described first paragraph liquefaction branch road M01 is for being connected in successively the first compressor C1 and the first cooler D1 behind the first distributing valve T1;
Be connected in the second cleaner P2 on described the first cooler D1 export pipeline, described second cleaner P2 links to each other with the high-pressure channel of the first Recuperative heat exchanger H1; High-pressure channel export pipeline at the first Recuperative heat exchanger H1 is installed the second distributing valve T2, and the high-pressure channel export pipeline of described the first Recuperative heat exchanger H1 is divided into second segment liquefaction branch road M02 and main cold branch road M2 two-way through this second distributing valve T2; Described second segment liquefaction branch road M02 is for being connected in successively high-pressure channel, first throttle bloating plant V1 and the gas-liquid separator S1 of the second Recuperative heat exchanger H2 behind the second distributing valve T2; The cold branch road M2 of described master is for being connected in successively high-pressure channel, the low-pressure channel of the second throttling bloating plant V2, the second Recuperative heat exchanger H2, the low-pressure channel of the first Recuperative heat exchanger H2 and the low pressure pipeline of gas pipeline of the second Recuperative heat exchanger H2 behind the second distributing valve T2;
The outlet of described gas-liquid separator S1 bottom is the LNG product outlet, and the outlet of gas-liquid separator S1 top connects the low-pressure channel of the second Recuperative heat exchanger H2, the low-pressure channel of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively;
The first precooling branch road M1 is the first decompressor E1 that is connected in the first distributing valve T1, and this first decompressor E1 connects the low-voltage tube passage of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively; Described the first decompressor E1 provides driving force for described the first compressor C1.
The second provided by the invention utilizes pipeline pressure can produce the liquefaction system of LNG, also can comprise the 3rd Recuperative heat exchanger H3, the second compressor C2, the second cooler D2 and the second precooling branch road M3; The first throttle bloating plant V1 of described the second liquefaction branch road M02 is choke valve; The second throttling bloating plant V2 of the cold branch road M2 of described master is the second decompressor E2;
Described the 3rd Recuperative heat exchanger H3 is arranged at described the first Recuperative heat exchanger H1 and and between the Recuperative heat exchanger H2; Connecting line between first class purification device P1 and the second compressor D2 is provided with the 3rd distributing valve T3, is divided into two pipelines behind the 3rd distributing valve T3, and this two pipeline is the 3rd section liquefaction branch road M03 and the second precooling branch road M3;
Described the second compressor C2 and the second cooler D2 are connected between the pressure piping of the 3rd distributing valve T3 and the first Recuperative heat exchanger H1 successively;
The 3rd section liquefaction branch road M03 is for being connected in successively the pressure piping of the second compressor C2 on the connecting line, the second cooler D2, the first Recuperative heat exchanger H1 between the 3rd distributing valve T3 and the second distributing valve T2 and the pressure piping of the 3rd Recuperative heat exchanger H3; The pressure piping outlet of described the 3rd Recuperative heat exchanger H3 is connected with described the second distributing valve T2;
Described precooling branch road M3 is the pressure piping that is connected to the first Recuperative heat exchanger H1 behind the 3rd distributing valve T3 in turn, the low pressure pipeline of the second decompressor E2, the 3rd Recuperative heat exchanger H3, the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline; The work done during compression of described the second compressor C2 is from the expansion work of the second decompressor E2.
Described the first cooler D1 and the second cooler D2 are water-cooling cooler or air-cooled cooler; The cooler outlet natural gas temperature is 10～40 ℃.
The liquefaction system that utilizes pipeline pressure can produce LNG provided by the invention obtains cold by expanding from the natural gas of pressure duct, and the pressure energy of natural gas is converted into cold energy, realizes the liquefaction of part natural gas, produces the LNG product and stores or transport.Because the one-level precooling temperature is higher, this portion gas need not to do deep purifying, has alleviated purification pressure.The work done during compression of all compressors has reclaimed pressure energy from decompressor in this system, need not the additional energy input, and the LNG that produces can be used as commodity, also can be used for peak regulation and use.
Description of drawings
Fig. 1 is the system diagram that utilizes pipeline pressure can produce the liquefaction system of LNG of the present invention among the embodiment 1;
Fig. 2 is the system diagram that utilizes pipeline pressure can produce the liquefaction system of LNG of the present invention among the embodiment 2;
Fig. 3 is the system diagram that utilizes pipeline pressure can produce the liquefaction system of LNG of the present invention among the embodiment 3;
Fig. 4 is the system diagram that utilizes pipeline pressure can produce the liquefaction system of LNG of the present invention among the embodiment 4.
The specific embodiment
Below in conjunction with drawings and Examples the present invention is further elaborated.
Embodiment 1: as shown in Figure 1, the liquefaction system of the present embodiment 1 comprises first class purification device P1, second cleaner P2, the first compressor C1, the first cooler D1, the first decompressor E1, the first Recuperative heat exchanger H1, the second Recuperative heat exchanger H2, first throttle valve V1, the second choke valve V2 and gas-liquid separator S1;
Natural gas from pressure piping at first slightly purifies dehydration through first class purification device P1, then is divided into two-way behind the first distributing valve T1, and this two-way is respectively the first precooling branch road M1 and first paragraph liquefaction branch road M01;
The natural gas flow that enters first paragraph liquefaction branch road M01 flow through successively the first compressor C1 and the first cooler D1 compression and be cooled; Enter afterwards second cleaner P2, after sloughing acid gas and impurity obtain deep purifying in second cleaner P2, be divided into two-way behind the second distributing valve T2, this two-way is respectively main cold branch road M2 and second segment liquefaction branch road M02;
The natural gas flow that enters second segment liquefaction branch road M02 flow through successively article one high-pressure channel of the first Recuperative heat exchanger H1 and article one high-pressure channel of the second regenerator H2 are then through entering gas-liquid separator S1 after the first throttle valve V1 throttling; Liquid among the gas-liquid separator S1 flows out by pipeline TK from gas-liquid separator S1 lower part outlet, be the LNG that produces, gas among the gas-liquid separator S1 flows out from the outlet of gas-liquid separator S1 top, article one low-pressure channel of article one low-pressure channel of the second Recuperative heat exchanger H2 and the first Recuperative heat exchanger H1 of flowing through successively reclaims cold, finally enters low pressure pipeline;
Flow into the 3rd the low-pressure channel recovery cold that the natural gas flow among the first precooling branch road M1 expands and passes through afterwards the first Recuperative heat exchanger H1 in the first decompressor E1, finally enter low pressure pipeline;
Flow into main cold branch road M2 natural gas flow successively by the second high-pressure channel of the first Recuperative heat exchanger H1 and the second high-pressure channel of the second Recuperative heat exchanger H2, then through after the second choke valve V2 throttling expansion, reclaim cold through the second low-pressure channel of the second Recuperative heat exchanger H2 and the second low-pressure channel of the first Recuperative heat exchanger H1 successively again, finally enter low pressure pipeline.
The driving of described the first compressor C1 is from the expansion work of described the first decompressor E1;
The first distributing valve T1 of the present embodiment is positioned at first class purification device P1 exit, and the second distributing valve T2 is positioned at second cleaner P2 exit;
Natural Gas High-pressure Pipeline pressure in the present embodiment 1 is 4.1MPa, and low pressure pipeline is 0.58MPa, and gas discharge is 1705Nm
3Under the gas source condition of/h, can utilize pressure energy to produce 247Nm
3The LNG of/h, liquefied fraction are 14.5%, and required energy consumption is the cooling tower water pump energy consumption that adopts the cooler D1 of water-cooled only, and the liquefaction system that utilizes pipeline pressure can produce LNG of the present invention has higher reliability and adaptability, and operating cost is low.
Embodiment 2:
As shown in Figure 2, the present embodiment 2 is with the difference of embodiment 1:
The second distributing valve T2 is between the first Recuperative heat exchanger H1 and the second Recuperative heat exchanger H2;
The second choke valve V2 export pipeline among the main cold branch road M2 connects into liquefaction branch road M02 at the d place of gas-liquid separator S1 top export pipeline; The e point place of the first decompressor E1 export pipeline of the first precooling branch road M1 between the first Recuperative heat exchanger H1 and the second Recuperative heat exchanger H2 connects into liquefaction branch road M02;
System's remainder is identical with embodiment 1.
System in the present embodiment 2 is with the advantage that embodiment 1 compares: the first Recuperative heat exchanger H1 is binary channels, the second Recuperative heat exchanger H2 is 3 passages, its manufacture difficulty and cost increase reliability and have reduced initial cost in the situation that do not change running effect all less than among the embodiment 1.
Embodiment 3:
As shown in Figure 3, the present embodiment 3 is with the difference of embodiment 1: throttling expansion equipment choosing the second decompressor E2 of main cold branch road M2, increased the second compressor C2 and the second cooler D2, and be specially:
After main cold branch road M2 isolates from the distributing valve T2 in second cleaner P2 exit, second high-pressure channel through the first Recuperative heat exchanger H1 enters the second decompressor E2, flow through the successively second low-pressure channel of the second Recuperative heat exchanger H2 and the second low-pressure channel of the first Recuperative heat exchanger H1 of natural gas after the second decompressor E2 expands reclaims cold, finally enters low pressure pipeline;
The natural gas of first paragraph liquefaction branch road M01 from second cleaner P2 out afterwards through behind the second compressor C2 and subsequent the second cooler D2, after entering again article one high-pressure channel of article one high-pressure channel of the first Recuperative heat exchanger H1 and the second Recuperative heat exchanger H2, behind first throttle valve V1, entering gas-liquid separator S1; The driving merit of the second compressor C2 is from the second decompressor E2;
Identical among system's remainder and the embodiment 1.
System in the present embodiment 3 with embodiment 1 under the identical gas source condition, can produce 324Nm
3The LNG of/h, liquefied fraction is 19%, is higher than the system among the embodiment 1.But owing to adopting two decompressors and double-compressor, system complexity is higher.
Embodiment 4:
As shown in Figure 4, the pipeline pressure that utilizes of the present embodiment 4 can be produced the liquefaction system of LNG, and its structure comprises:
With the first class purification device P1 that the outlet of gas pipeline pressure piping links to each other, be divided into first paragraph liquefaction branch road M01 and the first precooling branch road M1 two-way behind the first distributing valve T1 on this first class purification device P1 export pipeline; Described first paragraph liquefaction branch road M01 is for being connected in successively the first compressor C1 and the first cooler D1 behind the first distributing valve T1;
Be connected in the second cleaner P2 on described the first cooler D1 export pipeline, described second cleaner P2 links to each other with the pressure piping of the first Recuperative heat exchanger H1; Establish the second distributing valve T2 at the pressure piping export pipeline of the first Recuperative heat exchanger H1, be divided into second segment liquefaction branch road M02 and main cold branch road M2 two-way behind this second distributing valve T2; Described second segment liquefaction branch road M02 is for being connected in successively pressure piping, first throttle bloating plant V1 and the gas-liquid separator S1 of the second Recuperative heat exchanger H2 behind the second distributing valve T2; The cold branch road M2 of described master is for being connected in successively pressure piping, the low pressure pipeline of the second throttling bloating plant V2, the second Recuperative heat exchanger H2, the low pressure pipeline of the first Recuperative heat exchanger H2 and the low pressure pipeline of gas pipeline of the second Recuperative heat exchanger H2 behind the second distributing valve T2;
The outlet of described gas-liquid separator S1 bottom is the LNG product outlet, and the outlet of gas-liquid separator S1 top connects the low pressure pipeline of the second Recuperative heat exchanger H2, the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively;
The first precooling branch road M1 is the first decompressor E1 that is connected in the first distributing valve T1, and this first decompressor E1 connects the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline successively; Described the first decompressor E1 provides driving force for described the first compressor C1.
Its structure also can comprise the 3rd Recuperative heat exchanger H3, the second compressor C2, the second cooler D2 and the second precooling branch road M3; The second throttling bloating plant V2 of the cold branch road M2 of described master is the second decompressor E2;
Described the 3rd Recuperative heat exchanger H3 is arranged at described the first Recuperative heat exchanger H1 and and between the Recuperative heat exchanger H2; Connecting line between first class purification device P1 and the second compressor D2 is provided with the 3rd distributing valve T3, is divided into two pipelines behind the 3rd distributing valve T3, and this two pipeline is the 3rd section liquefaction branch road M03 and the second precooling branch road M3;
Described the second compressor C2 and the second cooler D2 are connected between the pressure piping of the 3rd distributing valve T3 and the first Recuperative heat exchanger H1 successively;
The 3rd section liquefaction branch road M03 is for being connected in successively the pressure piping of the second compressor C2 on the connecting line, the second cooler D2, the first Recuperative heat exchanger H1 between the 3rd distributing valve T3 and the second distributing valve T2 and the pressure piping of the 3rd Recuperative heat exchanger H3; The pressure piping outlet of described the 3rd Recuperative heat exchanger H3 is connected with described the second distributing valve T2;
Described precooling branch road M3 is the pressure piping that is connected to the first Recuperative heat exchanger H1 behind the 3rd distributing valve T3 in turn, the low pressure pipeline of the second decompressor E2, the 3rd Recuperative heat exchanger H3, the low pressure pipeline of the first Recuperative heat exchanger H1 and the low pressure pipeline of gas pipeline; The work done during compression of described the second compressor C2 is from the expansion work of the second decompressor E2.
Described the first cooler D1 and the second cooler are water-cooling cooler or air-cooled cooler; Gas pipeline pressure piping outlet temperature is 10～40 ℃.Described first throttle bloating plant V1 is choke valve.
The pipeline pressure that utilizes shown in Figure 4 can be produced the liquefaction system of LNG, and its flow process is as follows:
Natural gas from pressure piping at first slightly purifies dehydration through first class purification device P1, then is divided into two-way behind the first distributing valve T1, and this two-way is respectively the first precooling branch road M1 and first paragraph liquefaction branch road M01;
The natural gas flow that enters first paragraph liquefaction branch road M01 is successively through the first compressor C1 and the first cooler D1 compression and be cooled, enter afterwards second cleaner P2, after in second cleaner P2, sloughing acid gas and impurity and obtaining deep purifying, be divided into two-way behind the 3rd distributing valve T3, this two-way is respectively the second precooling branch road M3 and the 3rd section liquefaction branch road M03;
The natural gas flow that enters the 3rd section liquefaction branch road M03 is successively through the second compressor C2 and the second cooler D2 compression and be cooled, then after entering article one high-pressure channel of article one high-pressure channel of the first Recuperative heat exchanger H1 and the 3rd regenerator H3, be divided into two-way behind the second distributing valve T2, this two-way is respectively main cold branch road M2 and second segment liquefaction branch road M02;
The natural gas flow that enters second segment liquefaction branch road M02 flows through article one high-pressure channel of the second regenerator H2, then through entering gas-liquid separator S1 after the first throttle valve V1 throttling; Liquid among the gas-liquid separator S1 flows out by pipeline TK from gas-liquid separator S1 lower part outlet, be the LNG that produces, gas among the gas-liquid separator S1 flows out from the outlet of gas-liquid separator S1 top, flow through successively article one low-pressure channel of article one low-pressure channel, the 3rd Recuperative heat exchanger H3 of the second Recuperative heat exchanger H2 and article one low-pressure channel of the first Recuperative heat exchanger H1 reclaims cold, finally enters the low pressure pipeline of natural gas;
The 3rd the low-pressure channel recovery cold that the natural gas flow that flows into the first precooling branch road M1 expands in the first decompressor E1 and passes through afterwards the first Recuperative heat exchanger H1 finally enters low pressure pipeline;
The natural gas flow that flows into main cold branch road M2 flows through the second high-pressure channel of the second Recuperative heat exchanger H2, then through after the second choke valve V2 throttling expansion, reclaim cold through the second low-pressure channel of the second Recuperative heat exchanger H2, the second low-pressure channel of the 3rd regenerator and the second low-pressure channel of the first Recuperative heat exchanger H1 successively again, finally enter the low pressure pipeline of natural gas.
The natural gas flow that flows into the second precooling branch road M3 second high-pressure channel of Recuperative heat exchanger H1 of at first flowing through, then enter the second decompressor E2, natural gas after the expansion reclaims cold through the 3rd low-pressure channel of the 3rd Recuperative heat exchanger H3 and the 4th low-pressure channel of the first Recuperative heat exchanger H1 successively, finally enters the natural gas low pressure pipeline.
System in the present embodiment 4 with embodiment 1 under the identical gas source condition, can produce 321Nm
3The LNG of/h, liquefied fraction are 18.8%.Equally, compare in embodiment 1, liquefied fraction is higher, and the pressure energy recovering effect is better, but owing to adopts two decompressors and double-compressor, system's relative complex.
Claims (8)
1. liquefaction system that utilizes pipeline pressure can produce LNG, it comprises:
The first class purification device (P1) that links to each other with the outlet of gas pipeline pressure piping, the first distributing valve (T1) is installed on described first class purification device (P1) export pipeline, and described first class purification device (P1) export pipeline is divided into first paragraph liquefaction branch road (M01) and the first precooling branch road (M1) two-way through this first distributing valve (T1); Described first paragraph liquefaction branch road (M01) is for being connected in successively the first compressor (C1) and first cooler (D1) of the first distributing valve (T1);
Be connected in the second cleaner (P2) on described the first cooler (D1) export pipeline, the second distributing valve (T2) is installed on described second cleaner (P2) export pipeline, described second cleaner (P2) export pipeline is through this second distributing valve (T2) minute two pipelines, and this two pipeline is second segment liquefaction branch road (M02) and main cold branch road (M2); Described second segment liquefaction branch road (M02) is for being connected in successively the high-pressure channel of first Recuperative heat exchanger (H1) of the second distributing valve (T2), high-pressure channel, first throttle bloating plant (V1) and the gas-liquid separator (S1) of the second Recuperative heat exchanger (H2); The cold branch road of described master (M2) is for being connected in successively the high-pressure channel of first Recuperative heat exchanger (H1) of the second distributing valve (T2), high-pressure channel, the second throttling bloating plant (V2), the low-pressure channel of the second Recuperative heat exchanger (H2), the low-pressure channel of the first Recuperative heat exchanger (H2) and the low pressure pipeline of gas pipeline of the second Recuperative heat exchanger (H2);
The outlet of described gas-liquid separator (S1) bottom is the LNG product outlet, and the outlet of gas-liquid separator (S1) top connects the low-pressure channel of the second Recuperative heat exchanger (H2), the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline successively;
The first precooling branch road (M1) is for being connected in first decompressor (E1) of the first distributing valve (T1), and this first decompressor (E1) connects the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline successively; The work done during compression of described the first compressor (C1) is from the expansion work of the first decompressor (E1).
2. according to the liquefaction system that utilizes pipeline pressure can produce LNG claimed in claim 1, it is characterized in that, described first throttle bloating plant (V1) is choke valve.
3. according to the liquefaction system that utilizes pipeline pressure can produce LNG claimed in claim 1, it is characterized in that, also comprise the second compressor (C2) and the second cooler (D2), described the second throttling bloating plant (V2) is the second decompressor (E2); Described the second compressor (C2) and the second cooler (D2) are connected between the second distributing valve (T2) and described the first Recuperative heat exchanger (H1) high-pressure channel on the pipeline successively; The work done during compression of described the second compressor (C2) is from the expansion work of the second decompressor (E2).
4. according to the liquefaction system that utilizes pipeline pressure can produce LNG claimed in claim 1, it is characterized in that, described the first cooler (D1) and the second cooler (D2) are water-cooling cooler or air-cooled cooler; The cooler outlet natural gas temperature is 10～40 ℃.
5. liquefaction system that utilizes pipeline pressure can produce LNG, it comprises:
The first class purification device (P1) that links to each other with the outlet of gas pipeline pressure piping, the first distributing valve (T1) is installed on described first class purification device (P1) export pipeline, and described first class purification device (P1) export pipeline is divided into first paragraph liquefaction branch road (M01) and the first precooling branch road (M1) two-way through the first distributing valve (T1); Described first paragraph liquefaction branch road (M01) is for being connected in successively the first compressor (C1) and first cooler (D1) of the first distributing valve (T1);
Be connected in the second cleaner (P2) on described the first cooler (D1) export pipeline, described second cleaner (P2) links to each other with the high-pressure channel of the first Recuperative heat exchanger (H1); High-pressure channel export pipeline at the first Recuperative heat exchanger (H1) is installed the second distributing valve (T2), and the high-pressure channel export pipeline of described the first Recuperative heat exchanger (H1) is divided into second segment liquefaction branch road (M02) and main cold branch road (M2) two-way through this second distributing valve (T2); Described second segment liquefaction branch road (M02) is for being connected in successively high-pressure channel, first throttle bloating plant (V1) and the gas-liquid separator (S1) of second Recuperative heat exchanger (H2) of the second distributing valve (T2); The cold branch road of described master (M2) is for being connected in successively high-pressure channel, the second throttling bloating plant (V2), the low-pressure channel of the second Recuperative heat exchanger (H2), the low-pressure channel of the first Recuperative heat exchanger (H2) and the low pressure pipeline of gas pipeline of second Recuperative heat exchanger (H2) of the second distributing valve (T2);
The outlet of described gas-liquid separator (S1) bottom is the LNG product outlet, and the outlet of gas-liquid separator (S1) top connects the low-pressure channel of the second Recuperative heat exchanger (H2), the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline successively;
The first precooling branch road (M1) is for being connected in first decompressor (E1) of the first distributing valve (T1), and this first decompressor (E1) connects the low-voltage tube passage of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline successively; Described the first decompressor (E1) provides driving force for described the first compressor (C1).
6. according to the liquefaction system that utilizes pipeline pressure can produce LNG claimed in claim 5, it is characterized in that, also comprise the 3rd Recuperative heat exchanger (H3), the second compressor (C2), the second cooler (D2) and the second precooling branch road (M3); First throttle bloating plant (V1) in the described second segment liquefaction branch road (M02) is choke valve; The second throttling bloating plant (V2) of the cold branch road of described master (M2) is the second decompressor (E2);
Described the 3rd Recuperative heat exchanger (H3) is arranged between described the first Recuperative heat exchanger (H1) and the second Recuperative heat exchanger (H2); Connecting line between first class purification device (P1) and the second compressor (D2) is provided with the 3rd distributing valve (T3), and the 3rd distributing valve (T3) is divided into two pipelines, and this two pipeline is the 3rd section liquefaction branch road (M03) and the second precooling branch road (M3);
Described the second compressor (C2) and the second cooler (D2) are connected between the high-pressure channel of the 3rd distributing valve (T3) and the first Recuperative heat exchanger (H1) successively;
The 3rd section liquefaction branch road (M03) threaded a pipe for being connected in the high-pressure channel of the second compressor (C2) on the connecting line, the second cooler (D2), the first Recuperative heat exchanger (H1) between the 3rd distributing valve (T3) and the second distributing valve (T2) and the height of the 3rd Recuperative heat exchanger (H3) successively; The high-pressure channel outlet of described the 3rd Recuperative heat exchanger (H3) is connected with described the second distributing valve (T2);
Described precooling branch road (M3) is for being connected to high-pressure channel, the second decompressor (E2), the low-pressure channel of the 3rd Recuperative heat exchanger (H3), the low-pressure channel of the first Recuperative heat exchanger (H1) and the low pressure pipeline of gas pipeline in first Recuperative heat exchanger (H1) of the 3rd distributing valve (T3) in turn; The work done during compression of described the second compressor (C2) is from the expansion work of the second decompressor (E2).
7. according to the liquefaction system that utilizes pipeline pressure can produce LNG claimed in claim 5, it is characterized in that, described the first cooler (D1) and the second cooler (D2) are water-cooling cooler or air-cooled cooler; The cooler outlet natural gas temperature is 10～40 ℃.
8. according to the liquefaction system that utilizes pipeline pressure can produce LNG claimed in claim 5, it is characterized in that, described first throttle bloating plant (V1) is choke valve.
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